WO2012085880A2 - Installation modulaire permettant de réaliser des procédés de conversion de matrices carbonées - Google Patents

Installation modulaire permettant de réaliser des procédés de conversion de matrices carbonées Download PDF

Info

Publication number
WO2012085880A2
WO2012085880A2 PCT/IB2011/055907 IB2011055907W WO2012085880A2 WO 2012085880 A2 WO2012085880 A2 WO 2012085880A2 IB 2011055907 W IB2011055907 W IB 2011055907W WO 2012085880 A2 WO2012085880 A2 WO 2012085880A2
Authority
WO
WIPO (PCT)
Prior art keywords
plant according
carbonaceous
reactor
conversion
previous
Prior art date
Application number
PCT/IB2011/055907
Other languages
English (en)
Other versions
WO2012085880A3 (fr
Inventor
Vander Tumiatti
Michela Tumiatti
Shubhender Kapila
Francesco Lenzi
Carlo Roggero
Original Assignee
Sea Marconi Technologies Di Vander Tumiatti S.A.S.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sea Marconi Technologies Di Vander Tumiatti S.A.S. filed Critical Sea Marconi Technologies Di Vander Tumiatti S.A.S.
Priority to US13/992,198 priority Critical patent/US20130256113A1/en
Priority to CA2819327A priority patent/CA2819327A1/fr
Priority to EP11837305.9A priority patent/EP2655993B1/fr
Priority to BR112013015614A priority patent/BR112013015614A2/pt
Priority to ES11837305.9T priority patent/ES2691722T3/es
Priority to MX2013007253A priority patent/MX2013007253A/es
Publication of WO2012085880A2 publication Critical patent/WO2012085880A2/fr
Publication of WO2012085880A3 publication Critical patent/WO2012085880A3/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B1/00—Retorts
    • C10B1/10—Rotary retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/30—Other processes in rotary ovens or retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/14—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot liquids, e.g. molten metals
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C5/00—Production of pyroligneous acid distillation of wood, dry distillation of organic waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/083—Torrefaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/02—Rotary-drum furnaces, i.e. horizontal or slightly inclined of multiple-chamber or multiple-drum type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/32—Arrangement of devices for charging
    • F27B7/3205—Charging
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/33—Arrangement of devices for discharging
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • C10G2300/1007—Used oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1022—Fischer-Tropsch products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/20—Rotary drum furnace
    • F23G2203/209—Rotary drum furnace with variable inclination of rotation axis
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/508—Providing additional energy for combustion, e.g. by using supplementary heating
    • F23G2900/50801—Providing additional energy for combustion, e.g. by using supplementary heating using the heat from externally heated bodies, e.g. steel balls
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • This invention relates to a modular plant performing integrated processes for conversion of carbonaceous matrices to obtain and/or to increase the value of "derived products", such as “energetic or bio-energetic carriers” or “energy or bio-energy” with little or no negative impact on the environment by being "C02-neutral - C02n” or “C02-Negative - C02N” and/or "Zero Emissions - ZE".
  • the “conversion processes” are processes capable of modifying one or more physical, chemical, biological and toxicological properties of the carbonaceous matrices.
  • the conversion processes include physical, chemical, thermo-chemical, electro-chemical and bio-chemical: extraction (oils; liquids; active principles; essences, substances; tannins, cellulose, hemicelluloses, lignin, etc.); transesterification; chemical-physical decontamination; detoxification; dehalogenation; depolarization; synthesis of substances and organic and/or organ metallic compounds; phase transfer catalysis,; enzymatic catalysis; depolymerization; extraction with "Steam explosion - SE", drying/thermal desorption; torrefaction; pyrolysis; gasification; catalytic hydrothermal gasification; Gas to Liquid (GtL) or Biomass to Liquid (BtL) or combustion.
  • extraction oil; liquids; active principles; essences, substances; tannins, cellulose, hemicelluloses, lignin, etc.
  • Carbonaceous matrices can be solids, liquids and gases containing and/or contaminated by organic substances. Few selected but not limiting examples, are carbonaceous matrices including: biomasses, greases or by-products of animal processing; organic fraction of agricultural, municipal, industrial and hospital wastes; urban and industrial sewage sludge; tires and rubbers; polymeric, elastomeric materials, thermoplastics, duroplastics; bituminous or hydrocarbon impregnated sands; asphalt and tars; tar linings; contaminated soils; composite materials; Electrical and Electronic Wastes - RAEE (WEEE - Waste Electrical and Electronic Equipment); car-fluff (ASR - Automotive Shredder Residue); chemical and/or bacteriological residues of military applications.
  • ASR Automotive Shredder Residue
  • Biomasses as defined by European Directives, National and/or local Laws (e.g. European Directives 2001/77/CE, 2009/28/CE etc.) Among the environmental contaminants the following are considered as priorities: POPs (PCBs, PCDDs, PCDFs, PBBs, etc.); PAHs/PCAs; etc.
  • POPs PCBs, PCDDs, PCDFs, PBBs, etc.
  • PAHs/PCAs etc.
  • derived products include the carbonaceous matrices with enhanced value obtained through “processes of conversion”.
  • “derived products” are: solids (solids as they are and/or mixed in “Cocktails”) such as solid matrices and char from thermo-chemical processes as torrefaction and algal biomasses etc.); liquids (vegetable oils, oils from algal biomass, natural and/or synthetic esters, synthetic liquids, hydrocarbon oleous fractions etc.); gases (biogas, pyrolysis gas, syngas from gasification etc.).
  • Bio-energetic carriers are the biogenic carbonaceous matrices containing bioenergy at a higher energetic density with respect to the original material and that are usable as conversion intermediates in the bio-energy value chain to enhance the economic and environmental sustainability, the energetic efficiency and the logistics through applications that are performed in different times and locations.
  • Simple but not limiting examples of bio-energetic carriers are: biomasses (lignin cellulosic, algae etc.) pre-mixed solids; torrefied solids; vegetable carbons; biogenic oils; pyrolysis bio-liquids; bio-liquids from BtL or GtL processes; Biogas; biogenic gas from pyrolysis; biogenic syngas from gasification.
  • C0 2 -neutral - C0 2 n or "C0 2 -Negative - C0 2 N” is the global balance of C02 deriving from the processes of conversion of the biogenic carbonaceous matrices that determines the "Carbon Footprint” and the interactions between different compartments of the environments and reserves (“Carbon sink”) i.e. the atmosphere, the geosphere, the hydrosphere and the biosphere.
  • C0 2 is the unit of measure to evaluate the climatic effects in terms of Global Warming Potential (GWP), known as "Greenhouse Effect” in accordance with the protocols of the United Nations Environmental Program (UNEP).
  • GWP Global Warming Potential
  • C0 2 N is the “Carbon Sequestration”, through the production and use of vegetable carbon (BioChar) as agricultural amendment and “soil improver” capable of capturing C0 2 (“C0 2 Capture”) at a rate of approximately 3 kg of C02 equivalent for per kg of Biochar.
  • BioChar vegetable carbon
  • Zero emissions - ZE is the global balance of emissions deriving from the processes of conversion of carbonaceous matrices obtained through recycling or the chemical or biochemical conversion of the emissions themselves into “derived products” or “bio- energetic carriers".
  • a simple but not limiting example of "ZE” type process is the biochemical conversion of the typical combustion products (C0 2 , NO x , particulate, ashes, etc.) as micronutrients for the cultivation of algae in waste waters deriving from preceding processes of conversion. Implementation of process leads to a self-sustained and virtuous integrated process.
  • Haloclean ® is considered as the pioneer of "Intermediate Pyrolysis".
  • CA2351892 Al priority 29.06.2001
  • Peter B. Fransham "Process for the conversion of carbonaceous feedstock into liquid, char and gas" is described. The process is based on a tubular reactor in which the conversion of a hydrocarbon feedstock material into a liquid, solid and gaseous pyrolysis product, where the heat is provided by thermally conductive bodies.
  • DE-380 035 describes a process for the distillation of solid fuels done by a cylindrical rotating reactor that is open at the two ends: DE-380 035 criticizes, in fact, design solutions in which a cylindrical reactor is equipped with sealings at the two ends, dissuading irrefutably engineers in this sector to develop a reactor closed at the two ends. Also, the plant described in DE-380 035 includes only heating means of a thermally conductive carrier introduced into the reactor, excluding the presence of direct heating means of the reactor and without explaining that the internal screw is stationary with respect to the body of the reactor.
  • EP-0 086 488 describes a rotary kiln only a part of which is enclosed in a heating stationary housing, thus being fundamentally different from a rotary reactor fully enclosed by a stationary housing.
  • US-2 723 226 describes a low temperature carbonization process using a rotary reactor in which the ends protrude outside a stationary housing, so it is fundamentally different from a rotary reactor fully enclosed by a stationary housing. Moreover, such reactor does not described the presence of a feeding conduit inside it for a thermally conductive carrier in addition to the feeding conduit for the material to be carbonized.
  • a plant in Gussing uses a allothermal thermo-chemical conversion process based on dual fluidised bed gasification technology (FICFB - Fast Internally Circulating Fluidised Bed) in which the heat transfer medium is sand.
  • FICFB dual fluidised bed gasification technology
  • This plant represents the "State of the Art” in the gasification of biomasses with efficiencies up to 81 %, off which 25 % is used for as electric power generation ( ⁇ 2 MW).
  • the plant operation has been validated with availability exceeding 7500hours/year.
  • Critical factor I "Explosion and/or fire" - This criticality is induced by the explosive atmosphere that can be triggered when abnormal concentrations of oxygen and/or air are present in one or more sub-systems of the plant. This condition typically results from the lack of proper sealing and/or inefficient compartmenting of the reaction atmosphere with respect to the external atmosphere. The triggering may also occur due to uncontrolled exothermal reactions, reversible or permanent seizing (e.g. screw - heating body - external fixed cylinder) of mechanical components with moving interfaces that can generate localised overheating and very high temperatures and/or deformation with wear and/or damaging of transmission shafts and/or revolving and fixed seals.
  • reversible or permanent seizing e.g. screw - heating body - external fixed cylinder
  • LEL lower explosion limit
  • UML upper explosion limit
  • the limit concentration of oxygen depends upon the composition of the gas produced, humidity, temperature and pressure. For H 2 and CO at ambient temperature and pressure, the limit concentration is 4%.
  • Critical factor II "Irreversible seizing with blocking of the plant” - This criticality is characterised by the seizing between the transport components (e.g. screw) and the inner surface of the reactor/s when relative movements among contiguous parts are present. This criticality can trigger in case thermally conductive bodies made of hard materials are present. These bodies, for example metal spheres, can get lodged in the interspaces between contiguous moving components resulting in irreversible seizing.
  • Critical factor III "Wear, friction corrosion” - This criticality is characterised by wears, scratching and/or reversible seizing, that in practical operations, can be correlated to the transportation of the material by the screw and cylinder of the fixed or rotating reactor, i.e. when relative motions between the two components is present. Results are similar to those of Critical Factor II, but with a lower intensity. Irreversible corrosive phenomena of the metals can occur in presence of atmospheres rich in CO, C0 2 and other gaseous compounds containing Carbon when operating in the temperatures range from 350°C up to 800°C. These phenomena, designated as "metal dusting” cause the pulverisation of steel surfaces at to the point of contact leading to progressive deterioration of structural parts eventually causing their collapse.
  • Critical factor IV "Thermal exchange inefficiency" - This criticality is characterised by heating inefficiencies due to low surfaces available for heat transfer between the heating parts and matrices. Thermal inefficiency can also be amplified by inefficient recoveries of energy inside the plant.
  • Critical factor VI "Lack of mixing" -
  • the thermal profile can result from lack of thorough mixing of the carbonaceous matrix or inhomogeneous or lack of thorough interaction between the metal heating bodies and the carbonaceous matrix in the reactor.
  • mixing the material to be treated with the metal heating bodies and the movement of the screw is at best marginal, whereas it is predominant in the transportation function with the material that under the effect of gravity, remains at the bottom of the reactor.
  • thermo-chemical conversion of carbonaceous matrices can be negligible or inefficient due to the lack of an energetic milling action of the material to be treated.
  • Energetic milling is capable of increasing the exchange surface and enhancing intimate contact which in turn reduces the conversion time, the inhomogeneity of conversion and increase capability to promote reactions triggered by properly formulated additives.
  • the patents cited above recognize the importance of such requisite in terms of minimal particle dimensions but do not indicate any "milling" function and the operation practice demonstrates that a rotary furnace and/or a simple screw do not provide the dynamic conditions required to reach fragmentation. In fact, under the effect of gravity the material and the metal heating bodies remain resting on the bottom of the reactor.
  • Viscous and insoluble tars tend to clog the ducts and indeed represent the true "Achilles heel" in these plants and cogeneration systems (i.e. gas engines, turbines etc.).
  • the scope of this invention is to provide a plant capable of performing several integrated processes for conversion of carbonaceous matrices in compliance with the set requirements in the field of application and free from the troubles and critical factors that have not been recognised in the current plants.
  • the plant comprises a fully enclosed rotary reactor, except for the presence of inlet/outlet passages for the matrix and the thermally conductive carrier.
  • such reactor has a substantially cylindrical central body closed at the two ends respectively by a stationary fixed head and a head fixed to the central body.
  • such reactor is integrally enclosed by a stationary housing and is equipped with an inlet feeding conduit for a thermally conductive carrier that is different from the feeding conduit of the matrix to be treated.
  • the thermally conductive carrier is an integral and fundamental part of the plant in every operational phase. In fact, without the presence of this thermally conductive carrier re-circulating in the plant, the plant cannot reach the operational conditions.
  • Figure 1 is a layout representation of the basic module of the modular plant described in this invention.
  • Figures 2a-2g illustrate respectively the layout of internal devices that can be fixed inside the rotary reactor of the basic module shown in Figure 1.
  • FIGS 3a-3d illustrate respectively the layout of the driving modules of the basic module of the invention of Figure 1.
  • Figure 4 represents the layout of a possible configuration of the inside of the basic module equipped with progressive profile drawer devices.
  • Figure 5 represents layout of a possible configuration inside of the basic module equipped with screw with rotating distributor of liquid and/or gaseous matrices.
  • Figure 6 represents layout of an additional form of implementation of the basic module of the invention with a liquid as the thermally conductive carrier.
  • Figure 7 shows the layout of a possible controlled feeding module of the modular plant of the invention.
  • Figure 8 shows the general layout illustrating possible operational configurations of the modular plant of the invention.
  • Figure 9 shows the layout of a possible configuration of the modular plant with constituting modules placed in container for pyrogasification application.
  • Figure 10 shows the layout of a possible configuration of the rotors of the modules and the carbonaceous matrices feeding module inside the container for the pyrogasification application.
  • Casing or stationary body housing enclosing the controlled atmosphere reaction zone, including the two interface ends, of materials compatible with the conditions of the process.
  • Spheres and/or thermally conductive bodies and/or carriers are .
  • Interface and loading conduit of the spheres and/or thermally conductive bodies and/or carriers are provided.
  • Generic carbonaceous matrix to be converted entering the rotary reactor selected from among 69, 74, 100, 101, 1 13, 130 for different typologies and/or operational phases of the different conversion processes (see Figures 1, 7 and 8).
  • Hyper-dynamic mobile bed constituted by spheres and/or bodies and/or thermally conductive carriers 4 and generic carbonaceous matrix to be converted 6.
  • Electric heating device for start up/shutting down and emergency phases.
  • Possible sifting grid section (spheres and/or thermally conductive bodies - converted solid matrices).
  • Exit interface end (Output end) with stationary sealing system and interface for safety device against explosion and/or fire.
  • Converted carbonaceous matrix light fraction (liquid and/or gaseous).
  • Converted carbonaceous matrix heavy fraction (solid and/or liquid) interfaces and exit conduit 19 and spheres and/or bodies and/or thermally conductive bodies 4.
  • Optional chamber with concentrated irradiation device (ultrasounds, microwaves, radio frequency and/or electromagnetic fields).
  • Drawer device optional winglet and/or ploughshare profile.
  • Basket device containing filler bodies, with or without high catalytic surface.
  • Inlet for process fluids examples: air, oxygen, steam, extraction solvents etc.
  • Rotor stationary feeding head with holes for the passage of circulating molten metal molten metal level. Molten metal.
  • Passage chamber for the hot gases flowing along the properly winged external wall of the housing.
  • Rotor driving group with hollow shaft and spokes fixed to the rotor.
  • Cathode constituted by a bundle of pipes in ceramic material (YSZ) and provided with a superficial layer of Nickel alloy (Ni-YSZ).
  • Exit interface 58 for converted gaseous and/or liquid from carbonaceous matrices. Solid carbonaceous matrices and ashes.
  • Exit interface for solid carbonaceous matrices and ashes 60 Exit interface for solid carbonaceous matrices and ashes 60.
  • Metal oxides reduction and conversion chamber with concentrated irradiation device microwaves, radio frequency (RF), electromagnetic fields and/or power laser.
  • Optional heating zone with integration of concentrated irradiation device microwaves, radio frequency and/or electromagnetic fields.
  • Solid carbonaceous matrix for obtaining products (Coke and Bio-coke 126) to be stabilized and packaged in module N 103.
  • Interface for inlet of liquid and/or viscous carbonaceous matrices to be reconverted 121 Interface for inlet of liquid and/or viscous carbonaceous matrices to be reconverted 121.
  • Variable pitch feeding screw Feeding screw drive assembly.
  • Input - Homogenous solid, liquid and gaseous carbonaceous matrices for multi -phase process such as conversion (extraction, decontamination, catalysis, etc).
  • Module A controlled feeding, "cocktail” and pre-treatment of carbonaceous matrices.
  • Module N stabilization and packaging of solids.
  • Module B Selective extraction and/or multi-phase conversion.
  • Output - Products and derived bio-products liquid, solid and gaseous
  • extraction and/or decontamination Hydrocarbons, Mineral Oils, Vegetable Oils; Natural Esters etc.
  • glycerine glycerine
  • Module D Heating and/or sub-stoichiometric oxidation.
  • Module E Catalytic pyrogasification with molten metal.
  • Pyrolysis liquids (BioPyroLiq, PyroLiq) - Liquid carbonaceous matrix converted by pyrolysis.
  • Syngas - gaseous carbonaceous matrix converted by catalytic gasification Syngas - gaseous carbonaceous matrix converted by catalytic gasification.
  • Module H Photo bio reactor for microalgae.
  • Biogenic carbonaceous matrix - Algal biomass as is - intermediate for subsequent conversion in modules A 102 and B 105.
  • This invention relates to a modular plant capable of performing integrated processes for conversion of carbonaceous matrices into products suitable for varied applications in compliance with what indicated in the field of application and in its scope.
  • Products can be "energetic or bio-energetic carriers", “energy or bio- energy” (see Figure 8) as described below in the various modules A, B, C, D, E, F, G, H, I, L, M and N.
  • the assembly of modular plant suitable for conversion of carbonaceous substrates for varied applications is accomplished by the integration of several "basic models”.
  • the "basic module” (shown in Figure 1) satisfies the priority requisite of "Zero risk of seizing and low friction wear and absence of contiguous parts with relative motions" in rotor 9.
  • the basic module is also free from critical factors II and III, which and can be operated at temperature ranging from -200°C to 1200°C, at pressures ranging from 0.1 mbar up to 100 bar in continuous or discontinued mode.
  • the basic module is comprised of (at least in part) one or more of the following elements.
  • a rotary reactor or a process reactor 9 (hereafter designated as "rotor” 9) around a central longitudinal axis having an inclination from 0° through 45° with respect to an horizontal plane having a largely substantially tubular central body, with a circular or polygonal cross-section with a diameter over length ratio of up to 1 :15, closed by a first fixed head 8 feeding rotor 9, consisting of a conveyor preferably rotary sealed in the interface with the terminal side of rotor 9 and a second head fixed to the body that can be of smooth or equipped with sifting section 14 for the separation of thermally conductive carriers 4 from the generic carbonaceous matrix to be converted 6.
  • the body with fixed head for sealable separate introduction of the generic carbonaceous matrix to be converted 6 and the thermally conductive carriers 4.
  • the first conduit 7 in the fixed head is the inlet for generic carbonaceous matrix to be converted 6 into the reactor and the second conduit 5 is the inlet of thermally conductive carrier 4 into the reactor.
  • Rotor 9 is equipped on the integral head with securing points for the specific internal devices 11 29 capable of creating conversion bed 10 formed by thermally conductive carriers 4 and the generic carbonaceous matrix 6 intimately in contact between them.
  • the housing or fixed body 1 including ends 2 and 15 is made of material compatible with the process conditions. The design guarantees the sealing of the reaction atmosphere with respect to the external ambient.
  • the housing is covered with a thermal and sound proofing layer 12.
  • a heating device 13 facing the cylindrical reactor can be installed inside the proofing layer. Such heating device is used during the starting/shutting-down or emergency conditions.
  • At the ends 2 15 of fixed housing 1 are equipped respectively with flanges 3 16 for an easy access and maintenance: in particular, end 15 is equipped with interface for a safety device to prevent explosions and/or fire.
  • the devices include sensors for monitoring concentrations of gases and, when required, for introduction of an inert shielding gas into an expansion chamber.
  • Housing 1 is also provided with openings for the passage of heavy fraction derived from the converted carbonaceous matrices 19, for the passage of thermally conductive carriers 4 through the interface and conduit 20. As well as opening for the passage of liquid and/or gaseous light fraction derived from converted carbonaceous matrices 17.
  • the rotation drive and support group 22 of said reactor is located inside fixed housing 1 and is without internal mechanisms having a relative rotary motion with respect to said cylindrical body 9.
  • the said thermally conductive carriers 4 are comprised of a plurality of solid bodies, in particular metal spheres, or by a liquid chosen from the group consisting of molten metals 50 and/or alloys thereof, molten salts, liquefied cryogenic fluids and liquid substances at ambient temperature, such oils, single or multiphase aqueous solutions and organic fluids.
  • the spheres can be of metal base and/or its alloys (i.e.
  • the thermally conductive bodies 4 can be spherical or not, with functionalized surface of dimensions from 0.5mm up to 100mm, but preferably from 10 to 25mm when involving steel spheres, selectively used, properly heated/cooled to operate over temperatures ranging from -200°C up to +1000°C.
  • liquid state metal molten metal
  • they are Sn, Bi, Zn, Pb and Al and/or alloys thereof with metals with catalytic effect (i.e. Fe, Ni, Cr, Mn, Co, Ti, etc.), directly or indirectly heated/cooled by thermal exchange with another fluid.
  • the thermally conductive carriers compatible with the applications can be: cryogenic fluids down to -200°C (i.e.
  • aqueous solutions with suspended solids from -5 up to +90°C, mineral base oil, natural and/or synthetic esters, polyethylene glycols and polypropylene glycols and their mixtures, silicon and/or fluoridated fluids from -40°C to +320°C, molten salts and/or their mixtures with melting temperature up to 550°C, molten metals and/or alloys thereof with melting temperature up to +1200°C.
  • the thermally conductive carriers are heated or cooled in a continuous and closed-loop mode through contiguous reactor with the characteristics in accordance with claims 1 and 2.
  • the energy supply can be directly provided by the selective oxidation (partial or complete) of one fraction the carbonaceous matrices or one or more of the carbonaceous matrices produced 1 10 in the main reactor. In this manner the matrix itself is further converted in a confined and closed-circuit contiguous reactor with the possibility of creating a self-cleaning and self-sustained process from energy point of view.
  • Rotor 9 is equipped with appropriate securing points where an internal device 1 1 capable of interacting with said carbonaceous matrix to be converted 6 is fixed.
  • the said thermally conductive carrier 4 be able to prevent irreversible seizing with the blocking of the plant (Critical factor II).
  • the internal devices can be preferably of the simple drawer type 23 or with a progressive profile, ploughshare 24, wings 25, solid or perforated screw 26, solid or perforated spiral 27, or basket type containing the catalytic surface filling bodies 28.
  • solid or perforated screw 26 it can be equipped with solid or hollow shaft possibly perforated for the injection of process fluids coming from an appropriate rotating head inlet.
  • On each rotor 9 one or more internal devices are integrated. The devices are configured in different typologies optimized performance of the conversion processes referred to in the field of application and its scope.
  • Devices such as drawers 23, ploughshare 24 and wings 25 are fastened in a secure manner preferably with bars, in a quantity exceeding 2, going across the single devices being secured to the ends of rotor 9.
  • the bars provide for an easy installation and removal of the internal devices and constitute the guides for the insertion of simple spacers and possibly of curved containment shields of the reaction bed for the mechanical and anti-wear protection of the internal surface of rotor 9.
  • This configuration surprisingly provides a "Zero risk of seizing" condition since no component with relative motions between them are present inside rotor 9 that, considering the interaction of thermally conductive carriers such as metal spheres 4, cause abnormal wear on structural parts of the plant and irreversible seizing (see Critical factor II).
  • Internal devices 1 1 that are most prone higher wear, are made with easily removable parts and considered “expendable” materials and protect the structure of the rotor against excessive wear and corrosion (Critical factor III).
  • hyper-dynamic conditions can be realized in the bed comprised of generic carbonaceous matrix to be converted 6 and metal spheres and/or bodies and/or thermally conductive carriers 4 through the synergic action between one or more of the following functions simultaneously or sequentially: I - transfer or dissipation of heat ("transfer”); II - transportation of material ("transport”); III - mixing of material (“mixing”); IV - crushing of material ("milling”); V - catalytic action ("catalytic action”).
  • This device is fixed to rotor 9 and is capable of providing the longitudinally and synchronized inlet of said process fluid 33 in the conversion zone inside rotor 9.
  • This device is essentially comprised of: a fixed part 35 where the oxidizing agents and/or process fluids 33 required for the conversion reaction/s are introduced; a rotating seal 34 inserted between the fixed part and the rotating part ensuring the sealing; a rotary part 32.
  • the process fluids 33 in case of oxidation or gasification of the carbonaceous matrix, are composed of air, oxygen and/or steam, whereas in the case of other processes such as for example "Steam Explosion - SE" it could be just saturated steam.
  • Rotor 9 includes a drive and support group including at least one component chosen from among longitudinal rollers 37, motorized and synchronized 36 interacting by friction with the external surface of the body of rotor 9, a motorized pinion 39 engaging a ring gear secured to rotor 40, a motorized shaft mounted outside the mobile head in correspondence with the longitudinal axis and a flexible element, such as a belt or chain 44 connecting a drive shaft to an external surface of the reactor body.
  • the drive groups can be chosen in relation to the application among the possible drive and support configurations 36, 38, 41 , 43. To ensure the sealing in the drive shaft and in the rotation shaft of the rollers with appropriate rotating safety packing seals are provided these can be continuously flushed and monitored.
  • Rotor 9 can also perform both functions i.e. driving component and providing the structural support.
  • a characteristic of rotor 9 is the low torque activation requirement and which in turn leads to a lower energy consumption and a limited wear.
  • the rotor 9 is totally or partially comprised of the following elements (as indicated in Figure 6): rotor 9 driven, possibly, by hollow shaft and spikes 53 equipped with internal devices 27 spiral or winged type and external wings 51 for the re-circulation of molten metal 46; reaction ambient fixed containment housing 1 ; inlet interface end 2 with fixed sealing flange 3; interface and conduit 47 for the inlet of molten metal 46 and/or alloys thereof; pusher (or screw) actuated inlet device 45 for the generic carbonaceous matrix to be converted 6; locking-proof loading cone 48 with holes for the passage of circulating molten metal 46; winged passage chamber 52 for hot gases 57 for energy supply; exit interface end 15 with fixed sealing system and flange 16 for maintenance and possibly packing seal 56 for the installation of pipe bundle heat exchanger 54 in metal material or a cathode 55 constituted essentially
  • the solid carbonaceous matrix 66 74 106 107 130 to be converted can be supplied from the head directly into rotor 9 thus into the bath of molten metal 50. Possible liquids or gases can be injected from the same inlet head directly into the molten bath by the appropriate injection device 45. The separation of the ashes occurs by simple skimming 63 from the mass of molten metal.
  • the thermally conductive carrier, i.e. molten metal 46 is continuously thermostatically controlled by a thermostatic fluid 57 possibly produced by the combustion of part of the converted carbonaceous matrix 58 and that flows through a chamber that presents at least a part of external winged surface 52 in common with said housing 1 so that an energy self- sustained plant is created.
  • the thermal profile in the reactor as a result is homogeneous, thus proving a better control of the conversion conditions for the carbonaceous matrix.
  • the modular system can provide a plurality of basic modules configured for different fields of application and interconnected among them in series or parallel, which can be arranged into one or more containers, so that the handling and installation in the desired site is facilitated.
  • the layout for possible configurations is defined in Figure 8.
  • the modular plant can be configured with module A of which the main characteristics are listed in Figure 7.
  • Module A 102 - controlled feeding and pre-treatment, Cocktail it provides one or more among the key functions and/or the processes: 1 - formulation of stabilized and homogenized "Cocktail" from heterogeneous matrices as they are through mixing, pre-treatment; 2 - drying of the carbonaceous matrix; 3 - feeding of downstream reactors 109, 114 and 1 16 with dosing of solid, liquid and gaseous matrices to be converted; 4 - mechanical pre-treatment of solid feeding material for the reduction of volumes thus its apparent density; 5 - possible addition of additives, catalysts and/or conserving agents; 6 - feeding in controlled atmosphere for the elimination of oxygen/air thus separation/compartmenting at several levels (primary and secondary) of the reaction ambient from the external ambient; 7 - energy recovery; 8 - possible energy recovery of air and/or condensation water for reuse in the conversion processes; 9 - possible injection of liquid and/or gaseous fraction.
  • Products emerging from module A include: single and/or premixed "Cocktail” solids for derivative products (BioCok, Cok 126) 86 and/or compacted and pre-heated 100 for direct injection into rotor 9; recovered watery matrix from drying 72.
  • the main characteristics of the materials are: 1 - increased energy density, 2 - increased volumetric density; 3 - homogeneous granulometry; 4 - chemical-physical stability; 5 - targeted incorporation (when necessary for the type of conversion) of additives and/or specific catalysts and conserving agents (bactericides, anti-mildew and fungicides etc.).
  • Module A is mainly composed of the following elements or devices: containers, silos and dosing systems 67 for the different typologies of heterogeneous types of carbonaceous matrices as they are 66 coming possibly from systems or devices for the appropriate dimensional reduction, by mechanical sectioning (i.e.
  • the drying and pre-treatment phase is not required and the dried homogeneous carbonaceous matrix to be treated 73 is fed directly into loading and dosing hopper 78.
  • the transfer screw of the solid carbonaceous matrix 73 and/or 74 and/or additives/catalysts 77 it can facilitate the extraction of solid carbonaceous matrix 86 for derivative product (Cok and Biocok 126) stabilized and packaged in module N 103.
  • Module B 105 provides one or more of the following key functions and/or processes: 1 - thermo-chemical and/or chemical-physical conversion of solid and/or liquid and/or gaseous matrices that can operate from -200°C up to 400-500°C at atmospheric or negative(vacuum) or positive pressure; 2 - separation and/or reaction with cryogenic agents of heterogeneous matrices from metals (i.e. tires, electric and electronic wastes, composite materials in general etc.); 3
  • the rotary reactor can be configured in series (sequential) or parallel and can be positioned horizontal or sloping with an appropriate closed-loop circuit for the recirculation of the spheres and/or thermally conductive carriers exploiting the gravity for the possible introduction of gaseous (i.e. hydrogen, oxygen, nitrogen etc.) or liquid matrices (e.g. extraction solvents etc.) through distribution device 31.
  • Module B is fed by specific inlet device for the solid, liquid and gaseous carbonaceous matrix 101 as is for the multiphase conversion (extraction, decontamination, catalysis etc.).
  • the extraction, decontamination and/or detoxification processes can be assisted by concentrated irradiation devices (ultrasounds, microwaves, radio frequency, electromagnetic fields) 21 to reduce the times and to enhance the efficiency of the conversion processes.
  • Vegetable oils can be obtained with the extraction processes at different temperatures and for simple mechanical action ("mixing", "milling” under hyper-dynamic conditions) even in a single stage, i.e. without separation of the shell and/or stone (i.e. Jatropha Curcas). They can be used as help for the extraction of single or sequential solvents according to different polarities possibly assisted by concentrated irradiation device 21 with extraction yields (e.g. 95% for Jatropha Curcas).
  • the solvents can be continuously salvaged in a closed-loop circuit by a vacuum fraction distillation.
  • module B effective transesterification processes of vegetable oils and/or greases using methanol containing sodium metoxide can be realized through closed-loop re-circulation up to 60°C in the presence of thermally conductive carriers, thus under hyper-dynamic conditions in the reactor. Natural esters and glycerine are obtained. The glycerine, in particular, can be converted into biogenic material for the production of bio-liquids for use of biopolymers or bio-fuels.
  • the glycerine can be used as is as a stabilizing agent in pyrolysis liquids 1 17 to mitigate their tendency to polymerization or can be subject to purification.
  • Catalytic hydrogenation processes can convert glycerine into biogenic liquids, as indicated hereafter in Example III of this invention.
  • Liquids and/or gels can be obtained through conversion processes of polystyrene with temperatures up to 80-100°C with mono esters (i.e. derivatives from transesterification of vegetable oils) reducing at the same time the packaging volumes (up to 100 times and over). Tannins, active principles and extracts and/or bio-derivatives 108 can be obtained with selective extraction processes with solvents in a temperature range between 80 and 100°C possibly assisted by a concentrated irradiation device (ultrasounds, microwaves, radio frequency and/or electromagnetic fields) 21. Concentration extracts of cellulose, hemicellulose, lignin, etc.
  • the "Steam Explosion” process for the production of a liquid “bioenergetic carrier” can be realized by a cascade configuration with reactors equipped with appropriate devices and thermally conductive bodies, such as metal spheres, in order to improve the efficiency with hyper-dynamic conditions, at different process conditions and possibly assisted by a concentrated irradiation device (ultrasounds, microwaves, radio frequency and/or electromagnetic fields etc.) 21.
  • Decontamination, selective depolarization (acid compounds and/or sulphurized corrosives; for example, DBDS DiBenzylDiSulphide up to ⁇ 5mg kg "1 ) and dehalogenation and/or detoxification of technical liquids from POPs, including PCBs and PCAs, that are performed by particle supports, adsorbents, reagents and/or catalysts can be realised.
  • the quantity of these particle supports typically up to 5% in weight with respect to the oil can be mixed with or be made of particle supports based on aluminum silicates and/or activated carbon and/or zeolites in the dimensional range from 0,5 and 5mm and in the typical ratio from 50 to 70% in weight, or constituted completely by the supports listed, together with a mixture of inorganic bases with alkaline and basic and alkaline-earths (KOH, CaO, MgO, CaC0 3 ) in particle formulation from 0.2 to 5 mm with high surface in the typical ratio from 10 to 20% in weight, polyalkylene glycols with high molecular weight in particle form from 0.2 to 5 mm in the typical ratio from 10 to 20% in weight, spheres and/or thermally conductive carriers with high catalytic surface in a dimensional range of 0.5 to 5mm (preferably constituted by Fe, Ni, Al, Cu, Zn and/or alloys thereof).
  • KOH, CaO, MgO, CaC0 3 inorganic bases with alkaline
  • the operational conditions are in hyper-dynamic state in a temperature range from 50°C to 200°C preferably between 80°C and 100°C and under conditions of negative pressure (vacuum) that can get up to 0.1 mbar.
  • This process can also be extended to other types of technical liquids such as diathermic, hydraulic, lubricant, hardening and/or electro erosion.
  • This conversion can be assisted by a concentration irradiation device/s 21 to reduce reaction times and to enhance the yield.
  • This configuration is equipped with integrated controlled feeding devices with mechanical filtration up to 1 ⁇ .
  • One of the possible applications is for insulating liquids, in particular those used in electric transformers, reactors and other strategic equipment for the generation, transmission, distribution and use of power in general that can be performed by fixed or mobile plants, compact for on-site intervention in closed-loop circuit without even partially draining the transformer or equipment.
  • the saturated and/or spent particle supports can be re-functionalized for the recovery of the oil or other impregnating technical liquid with extraction process using solvent as described here above, while the particle support is subject to pyrolysis, in module C 109, up to 600°C for its full re-functionalization and recovery as an alternative to the current treatment processes by combustion in column or disposal as wastes by incineration or disposal in authorized landfill.
  • Tar sands containing hydrocarbons in general and/or contaminated soils in general can be converted by sequential extraction processes with solvents to obtain hydrocarbons or other carbonaceous matrices to be valorised.
  • WEEE wastes and/or car fluff (ASR) and /or composite materials in general it is possible to facilitate the separation of metals or other materials from the matrix as is to be converted under particular process conditions using cryogenic fluids such as liquid air or liquid nitrogen up to -200°C and more that make brittle the carbonaceous matrix as is thus facilitating the separation and the recovery of metals and materials contents (i.e. harmonic steel from used tires etc.).
  • thermo-chemical conversion processes of polypropylene and or primary and/or residual polystyrene in a temperature range of 300- 500°C in presence or not of specific catalysts to obtain a low viscosity liquid with high calorific value as "energetic carrier” or other applications.
  • halogenated compounds for example PBB (PolyBromoBiphenyl)
  • bromidic acid (HBr) bromidic acid
  • Module C 109 provides one or more among the following key functions and/or processes: 1 - thermo- chemical conversion from 200°C up to 900°C, depending upon the type of process to be implemented; 2 - torrefaction of biomasses between 200°C and 300°C with resident times between 1 min up to 60 min; 3 - pyrolysis of biomasses between 350°C and 700°C with residence time from 30s to 30min; 4 - pyrolysis of non-biogenic materials between 300°C and 750°C with resident times between lmin and 120min and higher; 5 - gasification of solid carbonaceous matrices between 700°C and 900°C with resident times between 2s and 10 min; 6 - minimization of the loss of pressure between the upstream and downstream parts of the module and operational pressure with slight depression with respect to the atmospheric one; 7 - Controlled atmosphere (i.e.
  • module C From module C it is possible to obtain mainly: biogenic torrefacts (BioTor 1 1 1), vegetable char (BioChar 11 1), solid from pyrolysis (Char 1 1 1), activated carbon (BioActCoal 11 1), pyrolysis liquid (BioPyroLiq, PyroLiq 1 17), pyrolysis gas (BioPyroGas, PyroGas 124), solid with high ferrous non-ferrous and noble metals content 1 1 1.
  • the torrefact presents the following main characteristics of "bio-energetic factors"": 1 - energetic density increased up to 30% more with respect to material; 2 - 35-40% volume reduction of the heterogeneous carbonaceous matrices as they are 66; 3 - 3% lower humidity in weight; 4 - elevated hydro-repelling properties; 5 - sterilization from bacteria, fungi, mildews and/or their consortia that otherwise could operate progressively diminishing the energetic content and incrementing the hygienic sanitary risks; 6 - elimination of self-combustion risks of stocks; 7 - easy dimensional reduction ("grindability") and homogeneity of the torrefied material; 8 - enhanced simplification, safety and profitability in the logistic chain (harvesting, transportation, stocking, use etc.); 9 - use of co-firing in general to reduce the C0 2 emissions of traditional combustion processes that use non-renewable sources; 10 - trading of certificates linked to the reduction of C0 2 emissions.
  • Vegetable char (BioChar 1 1 1) presenting the following main characteristics of "bio-energetic carriers" or as agricultural amendments: 1 - enhanced energetic density up to 76% more with respect to the heterogeneous solid carbonaceous matrix as is 66; 2 - possibility of use as agricultural amendment for the enhancing of yields up to 20% more; 3 - possibility of use in capturing C0 2 (since 1kg of biochar captures up to 3kg of C0 2 e) - "C0 2 -Negative - C0 2 N" 141 ; 4 - use in co-firing in general to reduce the emissions of C0 2 of traditional combustion processes using non-renewable sources; 5 - trading of certificates linked to the reduction of C0 2 emissions.
  • Biogenic activated carbons present the following main characteristics of "bio-energetic carriers”: 1 - elevated active superficial area up to 800-1000m 2 g " '; 2 - possibility of being formulated in different particle size (brickets, pellets, etc.) suitable for direct application or to be impregnated with specific catalysts (e.g. selective treatment of primary and/or drinking waters, treatment and filtration of vegetable and/or technical oils); 3 - possibility of being reintegrated by re-functionalization by pyrolysis processes assisted by concentration irradiation device (microwaves, radio frequency and/or electromagnetic fields).
  • Biogenic pyrolysis liquids (BioPyroLiq 117) present the following main characteristics as "bio-energetic carriers”: 1 - enhanced energetic density with respect to the heterogeneous solid carbonaceous matrix as is 66; 2 - enhanced simplification, safety and profitability in the logistic chain (harvesting, transportation, etc.); 3 - use in bio-refinery and use in energy cogeneration groups.
  • a special pyrolysis process is applied to the WEEE wastes chain and allows the simultaneous separation of the organic matrix in the liquid (PyroLiq 117) and/or gaseous (PyroGas 124) fraction, whereas the inorganic matrix results together with the solid carbonaceous matrix (Char 11 1) where the ferrous, non-ferrous and noble metals content concentrates facilitating the metallurgic and/or selective electrochemical recovery of metals that would be otherwise difficult to be extracted.
  • a dehalogenation and/or detoxification process of the halogenated compounds POPs that are present in the initial electric and electronic material as components of the polymeric material itself or as flame retardants (i.e.
  • contaminated soils i.e. soils, particle solid materials in general
  • tar sands i.e. soils, particle solid materials in general
  • the dehalogenation and detoxification processes of POPs use additives and/or catalysts such as CaO and/or CaC0 3 and/or KOH and/or MgCa(C0 3 ) 2 and/or ((Mg,Fe) 2 Si0 4 ) and/or ZnO and/or MnO and/or CuO and/or Fe 2 0 3 and/or MgO and/or MgC0 3 , oxide or hydroxide of alkaline metal and/or alkaline-earth and/or Ci-C 6 alcoholate of alkaline metal and/or alkaline-earth.
  • This process is classified as "Non-Combustion Technology" of residual material and/or wastes in general.
  • the modular plant can be configured as "module D 1 14 - heating and/or sub- stoichiometric oxidation" - that makes reference to the basic module described.
  • Module D 1 14 provides one or more among the following key functions and/or processes: 1 - heating of the spheres and/or thermally conductive carriers 4 in continuous mode and closed-loop with module C 109 itself; 2 - thermo-chemical conversion of torrefact or pyrolysis char 1 10 obtained from the conversion processes in module C 109; 3 - energetic self-sustaining of the main thermo-chemical conversion process from 300°C to 1050°C depending upon the temperature required in module C 109; 4 - minimization of the pressure loss between the upstream and downstream sides of the module and with operational pressures slightly in depression with respect to the atmospheric one and effective evacuation of the gas produced; 5 - oxidation of the carbonaceous matrix by selective and synchronized distribution of the process fluids 33 or of the oxidative gaseous or liquid agents 104 and 1 19; 6 - transportation, feeding and
  • thermo-chemical conversion process is taking place under sub-stoichiometric conditions, capable of generating the primary thermal energy totally satisfying the thermal demand of the entire modular plant and in particular of module C 109 for the heating of the spheres and/or thermally conductive carriers 4 constituting, de facto, the most efficient conversion system of carbonaceous matrices into thermal energy.
  • the injection and targeted distribution of oxidative agents is realized by a special rotary distributor device 31 previously described and indicated in Figure 2 and Figure 5.
  • the modular plant can be configured as "module E 1 16 - catalytic pyrogasification with molten metal" - that makes reference to the basic module described.
  • Module E 1 16 provides one or more among the following key functions and/or processes: 1 - direct and simplified thermo-chemical conversion under different isotherm conditions, if required, of solid, liquid and gaseous matrices with the use of molten metal and/or alloys thereof, in a temperature range from 250°C to 1200°C and more, but preferably up to 900°C; 2 - use of alloys of molten metal and/or alloys thereof with metals with catalytic effect; 3 - fractioned distillation, regeneration and/or re-refining of technical fluids with hydrocarbon base, natural and/or synthetic esters; 4 - integrated conversion of metal oxides into metal by a concentrated irradiation device (microwaves, radio frequency, electromagnetic fields and/or power laser) 64 in reducing ambient; 5 - application as a type MMA-SO
  • Module E is fed by a specific inlet device of the homogeneous solid carbonaceous matrix as is at low concentration of water 74. From module E are mainly obtained: syngas or Biosyngas 120, solid (Char o BioChar 1 1 1), ashes and micro nutrients 1 15, recovery watery matrices 104, high yield electric and/or thermal energy and/or bio-energy 132. In module E a molten metal and/or alloys thereof is used as thermally conductive carriers so that a more efficient thermal exchange carrier and catalytic effect are obtained. This provides a simplification of the processes and the compaction of the plant that make it applicable also for reduced productive capacities.
  • the oxygen that is intrinsically present in the carbonaceous matrices to be converted 6 reacts with the metals forming the relevant oxides. These oxides, generated by the reaction, float together with the char in the upper side of the reactor since they are lighter, and are collected into a restricted zone designated as "reduction chamber” 64 arranged on the surface of molten metal 50.
  • the metal oxides are intimately mixed with a carbonaceous matrix (Char) characterized by an elevated concentration of Carbon, thus capable of effectively absorbing the concentrated energy provided by a concentrated irradiation device (micro waves, radio frequency, electromagnetic fields and/or power laser) 64.
  • the electrochemical conversion ambient is essentially made of molten metal 50 continuously fed by an appropriate flow of solid, liquid and/or gaseous heterogeneous carbonaceous matrix (fuel) 6 and appropriately controlled in its content of oxygen.
  • the concentration of oxygen must be less than 2%, but preferably between 0.1-0.2%.
  • the fuel providing carbon to form H 2 and CO creates the condition to activate the electrochemical reactions of the fuel cell (e.g.
  • the cathode 55 is essentially made of a "cluster" of elementary cells (pipes) and the walls of each single cell are composed of two layers.
  • the first layer makes the electrolyte and is made with a special ceramic material, preferably Yttria-stabilized Zirconia (YSZ) and capable of permeating Oxygen ions
  • the second layer externally in contact with molten metal 50
  • YSZ Yttria-stabilized Zirconia
  • Ni-YSZ nickel alloy and ceramic material with Zirconium base
  • the typical electric performance of the single electric cell results is equivalent to 0.65 V/cell and the electric power equivalent to 1.5W/cm 2 .
  • the entire conversion reactor of the generic carbonaceous matrix 6 becomes an efficient and compact co-generation system with electric efficiency up to 52% and more and total efficiency up to 90%.
  • the operational temperature in the configuration MMA-SOFC is up to 1000°C.
  • the compactness of this solution allows an easier decentralized inter connection in electric grids "Smart Grids".
  • the initial carbonaceous matrix 6 with bases such as for example CaO and/or CaC0 3 , MgO and/or MgC0 3 , to neutralize and/or detoxify derivatives of Sulphur and halogenated organics with Chlorine, Fluorine, Bromine.
  • a modular plant with rotor 9 with molten metal is classified as a conversion process of heterogeneous carbonaceous matrices, for example halogenated ones, containing and/or contaminated by POPs including or not PCBs and other dangerous organic compounds, alternative to traditional incineration processes by high temperature combustion (1200°C with resident time >2s) characterizing itself as a "Non-Combustion Technology" for residual materials and/or wastes in general.
  • This application of the process that is carried out without inlet of oxidizing agent to prevent the formation of highly dangerous by-products (i.e.
  • PCDDs dioxins, PVDF-furans can be used under lower temperature conditions (in the range of 450-750°C) with catalytic action of the alloy of molten metals and possibly with the help of cooperating agents such as primary or secondary donors of hydrogen with the possible addition of CaO and/or CaC0 3 and/or KOH and/or MgCa(C0 3 ) and/or (Mg,Fe) 2 Si0 4 and/or ZnO and/or MnO and/or Fe 2 0 3 and/or MgO and/or MgC0 3 , oxide or hydroxide of alkaline metal and/or alkaline- earths and/or Ci-C 6 alcoholate of alkaline metal and/or alkaline- earths, obtaining the detoxification of POPs and the recovery of "Secondary Raw Materials" (e.g.
  • the modular plant can be configured as module F 118 - hyper-dynamic catalytic gasification - which makes reference to the basic module described here above.
  • Module F 118 provides one or more of the following key functions and/or processes: 1 - gasification of the converted volatile carbonaceous matrices 1 13 obtained by module C 109 and D 1 14 into permanent gas from 700°C up to 1200°C, preferably about 850-900°C by injection of oxidizing agents; 2 - catalytic action with the help of large surface catalysts under hyperdynamic conditions; 3 - minimization of the production of POPs/tars and acid compounds; 4 - minimization of the loss of pressure between the upstream and downstream of the module and with operational pressures slightly lower with respect to the atmospheric one (depression) and effective evacuation of the gases produced; 5 - self-cleaning conditions; 6 - easy evacuation of the ashes 115; 7 - production of multi-wall carbon nanotubes and hydrogen H 2 .
  • Module F 1 18 has a thermally conductive fluidized particle bed 128 possibly integrated with deposit of catalytic metal on the internal pores such as for example Nickel and/or its alloys.
  • a conveying device of the volatile converted carbonaceous matrices 1 13 (coming from module C 109) and possibly, gas produced by module D 1 14.
  • the reactor is equipped with rotary head for the injection of the oxidizing agent (air/Oxygen) 1 19 and steam 104 that triggers the required increment of temperature and that in a sub- stoichiometric concentration, convert into permanent gas the organic fractions interacting with the catalytic particle support making up the mobile bed 28.
  • oxidizing agent it uses the Oxygen rich gaseous matrix 119 coming from module H 127.
  • the rotor is also equipped with a feeding device of the particle support that it is typically made of sections of spiral 27 with counter rotating start fixed to rotor 9 itself and can provide the conveying in continuous mode the mobile catalytic bed 28 in the central section maximizing its height.
  • Specific devices can be present in the central section 11 suitable to ensure continuously the hyper-dynamic operational conditions and capable of procurzing the functional and energetic quality of the gas produced.
  • the conversion into permanent gas (Syngas 120) occurs with the help of mixture composed of metal based catalysts such as for example Ni, Cr, Mn, Fe, Co, Ti, etc. and/or alloys thereof. It can also be used additionally as integration as additives and catalysts oxides and/or silicates such as for example (Mg,Fe) 2 Si0 4 , MgCa(C0 3 ) 2 , SiC, activated A1 2 0 3, silica gel, etc. and neutralization additives for the acid compounds (i.e.
  • H 2 S, HBr, HC1, etc. such as for example KOH, CaO, MgO, CaC0 3 etc..
  • This configuration guarantees elevated conversion efficiency into syngas respecting what are the characteristics that distinguish a fluidized bed: optimized mixing of the bed, homogeneity of temperature, elevated heating speed of the organic vapours of the pyrolysis, possibility of adding additives and/or catalyzer, possibility of internal or external circulation of the material constituting the bed, intrinsic self-cleaning capacity.
  • To optimize the self-cleaning capacity the action of continuous friction in dynamic state is exploited both for the external and internal cleaning of the catalytic filling bodies.
  • the friction itself among the filling bodies ensures the cleaning of the external surfaces, whereas the auxiliary filling bodies (i.e.
  • Multi Wall Carbon NanoTubes can be obtained by dual stage catalytic conversion of the syngas at high temperature through the use of specific catalysts that can be ferrocene Fe(C 5 H 5 ) 2 and other metallorganic compounds and their derivatives, intermetallic compounds obtained from carbonates of Lanthanum, Neodymium and Nickel i.e. LaNi 5 e NdNi 5 that simultaneously produces a mixture with a high content of hydrogen which results being the main sub- product of the production of multi-wall carbon nanotubes.
  • specific catalysts can be ferrocene Fe(C 5 H 5 ) 2 and other metallorganic compounds and their derivatives, intermetallic compounds obtained from carbonates of Lanthanum, Neodymium and Nickel i.e. LaNi 5 e NdNi 5 that simultaneously produces a mixture with a high content of hydrogen which results being the main sub- product of the production of multi-wall carbon nanotubes.
  • Module G 122 provides one or more of the following key functions and/or processes: 1 - abatement of the gas temperature from 1000°C to temperatures compatible with the downstream use with low losses of pressure and under a slight depression; 2 - condensation of the liquid matrices at low temperature and possible regulation of the process temperature of the single phases based upon the dew point temperature of the condensables; 3 - removal of POPs, tars, NH 3 , solid particulate and other contaminants up to a concentration compatible with the application and environmental prescriptions; 4 - low energy consumption, maximized compactness and operational flexibility with elevated efficiency and easy energetic recovery of the heat removed.
  • Biosyngas or syngas 124 From module G are mainly obtained: Biosyngas or syngas 124, intermediate watery matrices 123, ashes and micronutrients 1 15 and carbonaceous matrices to be converted 121 and pyrolysis liquid (BioPyroLiq and PyroLiq 1 17).
  • the syngas and/or Biosyngas 124 are characterized by "POPs & tars Free" 143, i.e. they present a concentration of contaminants below what is prescribed by local norms and by the requisites imposed by the downstream applications. For what the tars are concerned, levels below 50mg/Nm 3 are achieved and for NH 3 values below 25mg/Nm 3 .
  • the modular plant from which the converted carbonaceous matrices 1 17 and 124 are obtained is characterized by the low environmental impact in terms of low total emissions into the atmosphere 139.
  • the modular plant can be configured with "module H - photo-bio-reactor for microalgae" - that is located downstream of the other modules making up the plant.
  • Module H provides one or more of the following key functions and/or processes: 1 - integrated conversion of the gaseous emissions of the upstream primary thermo-chemical processes with "Zero Emissions - ZE" 142; 2 - biochemical conversion of carbonaceous matrices by photosynthesis of the C0 2 obtained from the processes and/or cogeneration systems (CHP), of the ⁇ compounds and particulate, of the micro elements contained by the pyrogasification ashes, of the carbonaceous matrices contained by the process waters and the recovery of energy; 3 - realization of a virtuous localized self-production cycle; 4 - on- site production of Oxygen as derivative product from cultivation of algal biomass; 5 - containerizable , compact module, with devices for the growth intensification of micro algae stocks.
  • CHP cogeneration systems
  • module H From module H are mainly obtained: primary algal biomasses 130; gases at very high concentration of Oxygen 1 19.
  • the primary algal biomasses 130 can be dried in module A 102 and lyophilised, packaged (as powder, granulate, pellets etc.) in module N 103 to make up an algal biomass derivative product 136 to be used as food integrator (for animals, fish farming etc.) or as "bio-energetic carriers".
  • the module is compact, stackable and containerizable in series or parallel, and has tubular reactors equipped with integrated lighting by cycles of artificial light optimized for the cultivation of algae stocks in general that is further intensified by the combined action of bio-electric stimulation and the targeted inoculation of micronutrients with specific chelating agents.
  • the modular plant can be configured as "module I 133 - interface for various modules".
  • the modules described here above must be properly interfaced with one or more of the following external modules: 1 - utilities module for energetic and electric continuity in case of emergency; 2 - device for the blowing-in of inert gas for regulated shutdown in order to prevent the formation of potentially explosive conditions and their possible triggering; 3 - combustion and treatment device of the emissions (i.e. pyrolytic torch) in case of start up/shut-down of the plant or emergency including system of controlled conveying of accidental emissions; 4 - supervision and monitoring of the various conversion processes in remote and redundant mode including module for diagnostics, e-Maintenance and e-Learning in remote modality as well (Web-based).
  • the modular plant can be configured as "module L 131 - Cogeneration module (CHP) - that makes the modular plant able to operate autonomously and simultaneously supply electric power to the grid, thermal and/or refrigerating power 132 possibly into "Smart electric grids".
  • the cogeneration module for the production of electric, thermal and/or refrigerating energy 132 can be made with the help of endothermic engine (gas, liquid fuels, “dual fuel” etc.), Stirling engines, gas turbine; fuel cells (SOFC independent and/or through integration with module I), ORC (Organic Rankine Cycle) turbo generator, etc.
  • the modular plant can be configured as "module M 134 - micro GTL (Fischer-Tropsch)" - that derives from the basic module, capable of producing advanced liquids (intermediates for chemistry, pharmaceutics, cosmetics, etc.) and quality "bio-energetic carriers”.
  • This conversion process GTL occurs in the presence of particle metal catalysts in suspension and with a syngas that shows a H 2 /CO ratio of about 1.5-2 times and possibly helped by the presence of an oils liquid carrier and/or helped by a concentrated irradiation device (microwaves, radio frequency, electromagnetic fields) 21.
  • the modular plant can be configured as "module N 103 - stabilization and packaging" - including one or more devices for the packaging by compression (granulate, pellets, brickets, stocks, etc.) and/or lyophilisation of the "derived products” and "energetic and bio-energetic carriers".
  • Module N is fed with solid carbonaceous matrix for derivative product (Cok and Biocok 126) and/or with heavy carbonaceous matrix 19 coming from the torrefaction, pyrolysis treatments, etc. for derivative products (BioTor, Biochar 1 1 1, carbon black 1 12).
  • the stabilization, homogenization and safety packaging are done for the classification, finalized for the safety card (REACH), for handling, transportation of dangerous goods (ADR, IMCO, etc.) and for use.
  • This module is strategic toward the prevention of unreasonable risks for workers, public health and the environment and in particular for accidental events caused by self-combustion, explosion and fire (e.g. non compacted pyrolysis char).
  • Rotary reactor and thermal exchange provided by steel spheres as thermally conductive carrier.
  • the first ones are inferior by a factor up to 50 times in terms of volume occupied with the same flow capacity and primary energetic demand.
  • the characteristics of this invention allow a drastic reduction of the conversion times and consequently the plant dimensions with the same delivery capacity of generic carbonaceous matrices to be converted 6.
  • An additional and decisive contribution to the enhancing of the global coefficient of thermal exchange is given by the hyper-dynamic state 10 in the reactor, the uniform distribution of the bed and the intimate contact with the carbonaceous matrix itself.
  • the hyper-dynamic state derives from the synergic action of the internal organs 11 that provide the functions of transportation, "mixing”, “milling” and possibly catalytic action that characterizes the interaction with the metal spheres and/or the thermally conductive carriers 4 in rotor 9 ( Figure 4). This is more evident, for example, when compared with the Haloclean ® plant (EP 1354172 Al), where the carbonaceous matrix inside the rotary kiln is transported by a screw.
  • the hyper-dynamic conditions under which the conversion occurs in the reactor subject of this invention provide surprisingly a response to critical factor VII described above and solve the criticalities indicated also by patent WO2010130988 Al on the correlation between the dimensions of the particles and the contribution of heat that determines the efficiency of the thermo-chemical conversion according to the notorious relation tAT ⁇ Cd x where t is the time necessary for the conversion, ⁇ the temperature increment in the heart of the particle of carbonaceous matrix, C is a constant relative to the speed of advancement of the thermal front in the particle [s/m] and d x is the particle size index of the particle matrix.
  • the global coefficient of exchange in the conventional kiln is equivalent to the one considered in the case of presence of the spheres and/or thermally conductive carriers 4.
  • the use of steel spheres as thermally conductive carriers provides a thermal exchange much more efficient with respect to all those conversion systems using quartzous sand or similar ones. This involves a strong reduction of the volumes required, for example, in gasifiers with re-circulating fluid bed like the one in Gtissing (Austria) mentioned in this patent in the section State of the Technique.
  • the use of metal spheres prevents the criticality given by the formation of light particles deriving from the disaggregation of the sand.
  • This level of extraction is not complete and has, in any case, low efficiencies (about 30-38%) in weight).
  • the oil extracted requires a subsequent filtration and "degumming".
  • Another method of extraction uses one or more solvents, for example hexane, that provides an extraction efficiency greater than 90%» in weight on the total oil contained by the seed.
  • Jatropha Curcas One of the critical factors of the use of Jatropha Curcas is the extraction solid residue ("cake") at high toxicity for humans and animals of some compounds present in the seeds, among them some inhibitors of trypsin. Trypsin is indeed a fundamental enzyme in the digestion of proteins both in animal and human nutrition. Table II lists the concentrations of the toxic and anti-nutritional components in the de-oiled "cake” of some varieties of Jatropha Curcas and the "cake" from Soya seeds:
  • the liquid and solid ("cake") matrices are not directly usable for the purpose of human or animal nutrition.
  • the oil fraction finds applications mainly for a subsequent conversion into bio-diesel by transesterification.
  • the most toxic compounds are the "phorbol esters” - PE) and they are potential promoters of tumors in humans.
  • the rotary reactor with spheres it has been surprisingly verified that in a single stage it is possible to achieve the complete extraction of the phorbol esters. This occurs by the simultaneous phases of feeding the seed into a simplified module A 102, transportation and corresponding resident time, heating, "mixing” and “milling” inside module B 105 and thus under hyper-dynamic conditions.
  • This conversion can be assisted possibly by a concentrated irradiation device with ultrasounds 21 and can be in continuous or discontinuous mode in the presence of solvents including hexane, methanol, ethanol, isopropanol and acetonitrile.
  • solvents including hexane, methanol, ethanol, isopropanol and acetonitrile.
  • the procedure effected for the tests implemented the extraction of the oil by single solvents or sequential extraction with solvents of different polarities.
  • the solvent has been recovered in closed-loop by under vacuum evaporator and the oil has subsequently been quantified gravimetrically. Extraction is carried out with the solvents, decontamination and detoxification of the toxic compounds present in the solid matrix.
  • the subsequent transesterification of the fraction of oil is done with methanol containing 0.15% of sodium metoxide (CH 3 ONa) through the re-circulation in closed-loop at 60°C.
  • the transesterification has been monitored by TLC - Thin Layer Chromatography. Once all the triglycerides have been consumed, the methanol is recovered by under-vacuum distillation in closed-loop, while the part of transesterification in terms of sodium metoxide and methanol has been stoichiometrically consumed. Subsequently, the glycerine is removed and converted in a separate modality into biogenic products of a higher value. From the sequential extraction from the "cake” with different types of solvents the following concentrations of phorbol ester (PE) are obtained, as listed in Table III.
  • PE phorbol ester
  • the anti-nutrients listed in the preceding table are eliminated by a subsequent treatment of the "cake” through an enzymatic treatment or heating at 120°C for about one hour, better exploiting the thermal exchange provided by the thermally conductive bodies 4 intimately in contact with the "cake” to be treated 6.
  • the results obtained with this process are listed in Table IV.
  • Phorbol ester (toxic) [mg g " '] 3 - 6 0,1 1 ⁇ 0,01
  • the "toxic cake” can be converted by specific treatments into torrefied (BioTor 1 11) or BioChar 1 1 1 and/or syngas 125 and energy 132 directly on the production site and/or near the plantations.
  • the rotary reactor provides also a high efficiency in the transesterification of biogenic oils, such as Jatropha Curcas oil, soy oil, palm oil, etc. having mono hydric alcohols, such as methyl alcohol and ethylic alcohol.
  • biogenic oils such as Jatropha Curcas oil, soy oil, palm oil, etc. having mono hydric alcohols, such as methyl alcohol and ethylic alcohol.
  • the extended surface provided by the metal spheres makes necessary a smaller quantity of catalysts required by the reaction, that minimizes the formation of salty by-products and require a purification of the mono esters and the glycerine sub-product.
  • Derivative liquids from biogenic matrices such as alcohol 2- propanol, 1 ,2- propanediol and 1 -propanol usable as intermediates in other chemical processes or as bio- energetic carriers 108, can be obtained from the conversion of glycerine by the rotary reactor through the reduction by hydrogenation in the presence of catalysts such as Ni, Pd and Rh deposited on a high surface particle support (silica gel, activated allumina, activated carbon, zeolites, etc.) at a temperature of about 120°C and a pressure between 20 and 40 bar.
  • catalysts such as Ni, Pd and Rh deposited on a high surface particle support (silica gel, activated allumina, activated carbon, zeolites, etc.) at a temperature of about 120°C and a pressure between 20 and 40 bar.
  • the rotary reactor with spheres is usable for the conversion of residual polystyrene (i.e. deriving from packages) with mono esters, obtained from the transesterification in which the process brings a drastic reduction in volume (100 times or more) of the residual polyesters and is capable of producing liquids and/or gel 108 usable also as protective impregnators of smooth or porous surfaces or as "energetic carriers", in any case preventing the criticalities connected with the disposal of wastes otherwise bulky and not bio-degradable.
  • module B 105 In the specific case an integrated process of physical decontamination, chemical-physical selective depolarization, dehalogenation/detoxification from PCBs and POPs, corrosive compounds, acid polar compounds deriving from oxidation has been carried out in module B 105.
  • the results are complying with standard IEC 60422 ed.3-2005. This result has been obtained with the configuration of module B 105 at a temperature of 80-100°C with reagent equivalent to 2.5% in weight with respect to the oil.
  • a reagent constituted and formulated with particle supports based on silicates or aluminosilicates has been used in a dimensional range from 0.5 to 5 mm and in the typical ratio from 50 to 70% in weight, a mixture of inorganic bases with alkaline basic and alkaline-earth (KOH, CaO, MgO, CaC03) in particle formulation from 0.2 to 5 mm with high surface in the typical ratio from 10 to 20% in weight, polyalkylene glycols with high molecular weight under particle form between 0.2 and 5mm in the typical ratio from 10 to 20% in weight, spheres and/or thermally conductive carriers 104 metals at high catalytic surface in the dimensional range from 0.5 to 5mm (preferably constituted by Fe, Ni, Al, Cu e Zn and alloys thereof).
  • the process conditions are in hyper-dynamic state 10 in a temperature range between 50 to 120°C, preferably between 80 and 100°C and under vacuum conditions that can arrive up to O.lmbar, but preferably 2 mbar.
  • the oil is injected by a feeding device sending it directly into the rotor, located on the inlet end 2 and exits after the treatment through exit end 15.
  • the oil level is typically maintained at 50- 60% of the height on the diameter of rotor 9 under hyper-dynamic conditions.
  • a vacuum is maintained in order to continuously operate the degassing and dehumidification, or extracting the reaction volatile products, thus performing the integrated conversion in a more effective and fast manner, without the need for arranging perculation columns on particle supports, reagents and/or adsorbents.
  • the oil is subsequently filtered by mechanical filters at 2 or ⁇ ⁇ nominal.
  • the application described can also be extended to other types of technical fluids in general such as diathermic, hydraulic, lubricating, hardening processes and or electro erosion fluids.
  • the process temperature is about 280-300°C and the heat required is provided by the spheres and/or thermally conductive bodies 4 coming from module D 1 14 where they are heated or from an external source or from solid fraction 19 that is produced by the torrefaction itself.
  • the converted volatile carbonaceous matrix (torrefaction gas 113) produced during the torrefaction can, in any case, cover up to 80% of the energetic requirement of the process itself including the preliminary drying by hot gas flow 115.
  • the modular plant that operates the torrefaction process in accordance with the characteristics of this invention is compact, flexible and easily transportable.
  • Such features allow the implementation of a decentralized production strategy of biogenic torrefacts near plantations or forestry areas for the current forest cleaning from branches and bark for the prevention of fires, but also in forests involved by diseases of the plants or unforeseeable attacks by parasites such as "Mountain Pine Beetle” in North America.
  • a specific module B105 based on rotor 9 can be integrated for an application in the domain of pre-conversion of tires at low temperatures with cryogenic (e.g. liquid nitrogen, liquid air, etc.).
  • cryogenic e.g. liquid nitrogen, liquid air, etc.
  • the solution implemented in this example provide a response to the valorization of materials coming from the disposal of tires that determines an important critical factor under an environmental point of view, especially when there are large uncontrolled accumulations, in case of fires which can produce atmospheric emission with highly polluting and carcinogenic substances (smokes containing PCAs etc.).
  • This process provides the valorization in an intelligent and flexible manner of the various liquid fractions (fuel) (PyroLiq 117), solid "carbon black” 1 12 and gas (PyroGas 124), as process energetic support.
  • the particle size distribution of the "carbon black” 1 12 obtained from the conversion of used tires fall within those classified by Standard ASTM D 1765- 10.
  • An additional integration can be the use of all the organic fractions obtained from the pyrolysis in module F 118 for hyper-dynamic catalytic gasification in synthesis gaseous carbonaceous matrix (syngas 124).
  • This application can be effectively extended also to polymeric materials in general, such as polypropylene, halogenated and not polymeries, thermoplastics, thermo hardenings, etc.
  • Biochar 1 1 1 increases the energetic density of the biomass reaching up to values of calorific value of about 30.000kJ kg "1 with respect to a typical value of the starting biomass of 17-18.000kJ kg "1 with an enhancement of 76%.
  • the production of Biochar 11 1 has a positive global climatic impact since it decelerates the cycle of carbon, reducing the greenhouse effect gases (i.e. C0 2 ) contrary to what occurs with combustion.
  • Biochar 111 is visually presented as "carbon black” and is resisting chemical and biological degradation. It is characterized by its stability through time (up to several hundred years). Biochar 111 contains aromatic substances that present a strong interaction with mineral particles and a spongeous structure characterized by high O/C and surface/volume ratios, capable of holding conspicuous amounts of exchangeable cations. It can be scientifically predicted that for each kg of Biochar 111 (typically containing about 70-80% in weight of carbon) that is used "una tantum” in cultivation lands up to 3 kg of C0 2 are captured, since the carbon is no further available for a subsequent conversion cycle.
  • the soil used for such culture was made up of a mixture of blonde peats and clay and fertilizer 14-16-18 equivalent to 0.8kg m " and had a pH 5.5-6.2, an electrical conductivity (Dutch method 1 : 1.5 v/v) equivalent to 0.5- 0.9ms cm “1 , capacity for the air 10% v/v, water easily available 30% v/v, irrigation as required.
  • This activation process is realized in modules C 109 configured in cascade by heating up to 900°C in the rotary reactor with the injection of steam such to determine the effect of "Steam Explosion - SE” at cycles finalized toward creating an elevated superficial area up to 800m 2 g "1 and more.
  • steam Explosion - SE steam Explosion - SE
  • the activated carbon depending upon the type of application, can be formulated in different particle sizes and geometrical forms (e.g.
  • the activated carbon can be re- functionalized by the application of a pyrolysis possibly assisted by concentrated irradiation device with microwaves 21 capable of restoring the initial exchange surface and at the same time self-cleaning by degrading the undesired organic compounds inside the matrix itself.
  • This application can be advantageously used in the conversion of rice straw with a high ash content, to obtain Silicium of biogenic origin at high purity and high catalytic surface for adsorption or catalysis processes.
  • the oxidizing agent in the tests was made of a mixture of air 119 steam 104, but mixtures of air enriched with oxygen 1 19, coming from module H 127 can be used.
  • the modular plant relative to the pyrogasification application is based upon the integration of modules A 102, C 109, D 1 14, F 1 18, G 122, L 131 and I 133.
  • the pyrogasification process is subdivided into two macro-stages finalized towards the complete conversion of the biomass.
  • the operating temperatures are 500°C for the first stage, whereas the second stage operates at 850°C.
  • a first option can be the simultaneous production of Biochar 1 11 and quality gaseous carbonaceous matrix (Biosyngas 124).
  • the second option is to maximize the production of Biosyngas 124 only.
  • oxygen with technical purity grade can be used as oxidizing agent to have a very high quality syngas 124 in terms of greater calorific value and minimizing the content of NO x compounds.
  • this gasification minimizes the problems of elutriation of the finest particles (carbon and/or ashes) since the second stage is focused only on the volatile carbonaceous fraction, offering parallelly operational flexibility, since the conversion stages are separated.
  • this plant configuration has the feature of having a single point of emission of the cogeneration group, since the gaseous flow dedicated to heating remains confined inside the plant itself.
  • This application with biomasses can also be extended to other typologies of carbonaceous matrices deriving from residual polymeric materials, such as used tires, plastic and/or thermo-setting plastics.
  • An additional conversion application of heterogeneous solid carbonaceous matrices as they are 66 with the modular plant is the production at high temperature of MWCNT - MultiWall Carbon NanoTubes 138 for applications of advanced materials in the presence of catalyzers.
  • the modular plant for the application relative to MWCNT 138 and syngas 120 is based upon the integration of modules A 102, C 109, D 1 14, F 1 18, G 122, L 131 and I 133.
  • the production process of MWCNT 138 is subdivided into two macro stages finalized towards the complete conversion of the initial carbonaceous matrix into syngas 120 with residual material composed by ash only; that is, all the char is converted in the sub-stoichiometric oxidation stage.
  • the catalytic hyper-dynamic gasification is to be intended subdivided, in turn, into two conversion stages.
  • the first stage the conversion into syngas 120 with high quality and low content of tars takes place, followed by a second stage of simultaneous deposition of multiwall carbon nanotubes 138, using appropriate catalysts providing their formation.
  • the multiwall carbon nanotubes 138 shall be subsequently separated from the gaseous flow 120.
  • the typical catalysers can be those indicated in the detailed description of the invention Ni, CaO, CaC0 3 , ferrocene Fe(C 5 H 5 ) 2 and other metallorganic compounds and their derivatives, inter metallic compounds obtained from carbonates of Lanthanum, Neodymium and Nickel i.e.
  • the pyrolysis temperatures are preferably 500°C, whereas the conversion and deposition of the portion of the multiwall carbon nanotubes operates at about 900°C.
  • a syngas 138 with high concentration of Hydrogen is obtained.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention a trait à une installation modulaire, qui est constituée d'au moins un module de base et qui est appropriée pour convertir des matrices carbonées (6) en combustible ou autres produits utiles sans aucun impact négatif sur l'environnement. L'installation modulaire inclut un réacteur rotatif (9) qui est équipé d'un mécanisme d'entraînement rotatif (22) et d'un corps fixe (1). L'inclinaison du réacteur (9) avec l'axe longitudinal central de rotation peut varier de 0° à 45° par rapport à un plan horizontal. Le réacteur est constitué d'un corps central, sensiblement un cylindre qui est fermé au niveau de la première extrémité, l'extrémité d'entrée, au moyen d'une tête fixe (8) et au niveau de l'autre extrémité, l'extrémité de sortie, au moyen d'une tête qui est fixée sur le réacteur rotatif (9). L'extrémité d'entrée (8) contient deux conduits, l'un (7) pour l'introduction de la matrice carbonée (6) dans le réacteur rotatif et l'autre (5) pour l'introduction de vecteurs thermoconducteurs (4). Le réacteur rotatif (9) est dépourvu de composants internes qui fournissent un mouvement de rotation par rapport au corps cylindrique. Le corps de logement fixe (1) enveloppant le réacteur rotatif (9) assure l'étanchéité du réacteur et conserve l'intégrité de l'atmosphère du réacteur par rapport à l'atmosphère ambiante extérieure. Le logement est pourvu d'ouvertures pour le passage des premier et second orifices d'entrée, ainsi que d'une sortie destinée à la matrice carbonée convertie (17, 19) et au vecteur thermoconducteur (4).
PCT/IB2011/055907 2010-12-23 2011-12-22 Installation modulaire permettant de réaliser des procédés de conversion de matrices carbonées WO2012085880A2 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
US13/992,198 US20130256113A1 (en) 2010-12-23 2011-12-22 Modular plant for performing conversion processes of carbonaceous matrices
CA2819327A CA2819327A1 (fr) 2010-12-23 2011-12-22 Installation modulaire permettant de realiser des procedes de conversion de matrices carbonees
EP11837305.9A EP2655993B1 (fr) 2010-12-23 2011-12-22 Installation modulaire permettant de réaliser des procédés de conversion de matrices carbonées
BR112013015614A BR112013015614A2 (pt) 2010-12-23 2011-12-22 instalação modular para realizar processos de conversão de matrizes carbonáceas.
ES11837305.9T ES2691722T3 (es) 2010-12-23 2011-12-22 Planta modular para realizar procedimientos de conversión de matrices carbonáceas
MX2013007253A MX2013007253A (es) 2010-12-23 2011-12-22 Planta modular para realizar procedimientos de conversion de matrices carbonaceas.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITTO2010A001043 2010-12-23
ITTO2010A001043A IT1406771B1 (it) 2010-12-23 2010-12-23 Impianto modulare per la conduzione di procedimenti di conversione di matrici carboniose

Publications (2)

Publication Number Publication Date
WO2012085880A2 true WO2012085880A2 (fr) 2012-06-28
WO2012085880A3 WO2012085880A3 (fr) 2012-08-23

Family

ID=43737432

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2011/055907 WO2012085880A2 (fr) 2010-12-23 2011-12-22 Installation modulaire permettant de réaliser des procédés de conversion de matrices carbonées

Country Status (8)

Country Link
US (1) US20130256113A1 (fr)
EP (1) EP2655993B1 (fr)
BR (1) BR112013015614A2 (fr)
CA (1) CA2819327A1 (fr)
ES (1) ES2691722T3 (fr)
IT (1) IT1406771B1 (fr)
MX (1) MX2013007253A (fr)
WO (1) WO2012085880A2 (fr)

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102758919A (zh) * 2012-07-18 2012-10-31 苏忠 热解旋转滚筒的密封装置
WO2013077748A3 (fr) * 2011-11-21 2013-07-18 Carbonscape Limited Appareil et procédé pour traiter une biomasse
WO2013110944A1 (fr) * 2012-01-25 2013-08-01 Nov Downhole Eurasia Limited Traitement de matériaux contenant des hydrocarbures
WO2014008496A1 (fr) * 2012-07-06 2014-01-09 South Dakota State University Réacteur de pyrolyse catalytique à lit fluidisé rotatif
ITTO20120894A1 (it) * 2012-10-12 2014-04-13 Sea Marconi Technologies Di Vander Tumiatti S A S Procedimento di co-produzione di bioenergia e prodotti da conversione integrata di biomasse e rifiuti urbani
EP2789677A1 (fr) * 2013-04-12 2014-10-15 Kymi Baltic Consulting Oü Installation de torréfaction, son fonctionnement et son entretien
WO2014185957A1 (fr) * 2013-05-14 2014-11-20 Ciris Energy, Inc. Traitement de matières premières carbonées
WO2015005807A1 (fr) * 2013-07-12 2015-01-15 Fluid S.A. Procédé de conversion de biomasses en carburant renouvelable et machine destinée à la conversion de biomasses en carburant renouvelable
WO2014153570A3 (fr) * 2013-03-15 2015-02-19 Transtar Group, Ltd Système nouveau et amélioré pour le traitement de divers produits chimiques et matériaux
EP2687782A3 (fr) * 2012-07-21 2015-10-07 Tadeusz Bak Procédé de production d'électricité et de chaleur dans un processus de conversion thermique de différents types de déchets dans une installation intégrée et installation intégrée pour la production d'électricité
WO2015181713A1 (fr) * 2014-05-26 2015-12-03 Centro Sviluppo Materiali S.P.A. Procédé et appareil pour la production de gaz combustible obtenu par des plastiques usés
US9353476B2 (en) 2014-04-18 2016-05-31 Georgia-Pacific Containerboard Llc Method for recycling waste material with reduced odor emission
RU2587115C1 (ru) * 2014-12-25 2016-06-10 Открытое акционерное общество "Научно-исследовательский институт металлургической теплотехники" (ОАО "ВНИИМТ") Противоточная шахтная печь для обжига карбонатных материалов, отапливаемая газообразным топливом
EP2783764B1 (fr) 2013-03-28 2016-07-13 ELG Carbon Fibre International GmbH Installation de pyrolyse et procédé destinés à la récupération de fibres de carbone à partir de matières synthétiques contenant des fibres de carbone, et fibres de carbone récyclées
EP3023478A3 (fr) * 2014-11-19 2016-09-21 Embraer , S.A. Un procédé pour le recyclage de matériaux composites et un système pour le traitement de gazes d'échappement
EP2752445B1 (fr) 2011-08-30 2016-10-19 Carbon Fiber Recycle Industry Ltd. Dispositif et procédé de fabrication de fibres de carbone recyclées
CN111036014A (zh) * 2019-11-22 2020-04-21 中南林业科技大学 人造板干燥系统除尘装置
CN112246832A (zh) * 2020-09-28 2021-01-22 威尔能环保科技(苏州)有限公司 一种电池材料处理系统
DE102019216564A1 (de) * 2019-10-28 2021-04-29 Siemens Aktiengesellschaft Modulare Abfallbehandlungsanlage
CN113368857A (zh) * 2021-04-29 2021-09-10 中国环境科学研究院 体相金属间化合物负载催化剂的制备方法
WO2022140829A1 (fr) * 2020-12-30 2022-07-07 Petróleo Brasileiro S.A. - Petrobras Système modulaire de traitement d'effluents provenant du nettoyage de coques d'unités flottantes
EP4151702A1 (fr) 2021-09-17 2023-03-22 Alpha Trading S.p.A. Procédé de traitement thermique continu d'un flux de matière d'alimentation comprenant au moins une fraction de matière polymère et installation pour la mise en oeuvre de ce procédé
AU2020206092B2 (en) * 2019-01-08 2023-08-17 Jie Xiong Jonathan YEO Manufacturing facility

Families Citing this family (41)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9447326B2 (en) 2012-06-22 2016-09-20 Sundrop Fuels, Inc. Pretreatment of biomass using steam explosion methods before gasification
US9175235B2 (en) 2012-11-15 2015-11-03 University Of Georgia Research Foundation, Inc. Torrefaction reduction of coke formation on catalysts used in esterification and cracking of biofuels from pyrolysed lignocellulosic feedstocks
JP6319093B2 (ja) * 2012-12-05 2018-05-09 宇部興産株式会社 バイオマス固体燃料
CN103752583B (zh) * 2014-01-10 2016-08-17 中国环境科学研究院 卤代POPs废物处理系统
US10106753B1 (en) 2014-02-05 2018-10-23 Uschi M. Graham Coal gasification process with conversion of CO2 to oxygen gasifier feed producing carbon by-product
AU2015274197B2 (en) 2014-06-09 2019-07-04 Hatch Ltd. Plug flow reactor with internal recirculation fluidized bed
PL228362B1 (pl) * 2014-06-16 2018-03-30 Adam Handerek Sposób termicznego rozkładu odpadowych tworzyw sztucznych i/lub biomasy i instalacja do prowadzenia procesu
US9993799B2 (en) * 2014-10-09 2018-06-12 Blue Planet, Ltd. Continuous carbon sequestration material production methods and systems for practicing the same
WO2016157086A1 (fr) * 2015-04-01 2016-10-06 Atena Solution Srl Système compact et transportable pour la production de pellets
CN104877691A (zh) * 2015-04-29 2015-09-02 武汉光谷蓝焰新能源股份有限公司 一种生物质滚筒式炭化炉
DE102016201801A1 (de) 2015-11-21 2017-05-24 Suncoal Industries Gmbh Partikelförmiges Kohlenstoffmaterial herstellbar aus nachwachsenden Rohstoffen und Verfahren zu dessen Herstellung
US9850433B2 (en) * 2015-12-31 2017-12-26 Chz Technologies, Llc Multistage thermolysis method for safe and efficient conversion of E-waste materials
US9816033B2 (en) * 2015-12-31 2017-11-14 Chz Technologies, Llc Multistage thermolysis method for safe and efficient conversion of carpet/rug, polymeric materials and other waste sources
US10465120B1 (en) * 2016-09-12 2019-11-05 Michael Garjian Method and device with catalyst storage and delivery capsule for converting biomass into solid and gaseous components
RU2637490C1 (ru) * 2016-10-28 2017-12-05 Акционерное общество "Ордена Трудового Красного Знамени и ордена труда ЧССР опытное конструкторское бюро "ГИДРОПРЕСС" Устройство электрообогрева ванны для дезактивации
CN113801670A (zh) * 2016-12-12 2021-12-17 朱书红 一种物料加热装置
CA3048503A1 (fr) 2017-02-27 2018-08-30 Glanris Water Systems, Inc Filtres a balles de riz activees, milieux filtrants et procedes
CA3072383A1 (fr) * 2017-03-23 2018-09-27 Kenny VANREPPELEN Carbonisation et activation d'un materiau contenant du carbone
US20190048166A1 (en) * 2017-08-14 2019-02-14 Environmental Waste International, Inc. Hybrid processing of waste material
US10577550B2 (en) 2017-09-26 2020-03-03 Catherine J. Chagnot Continuously operable mechanical or electrical power source fueled by gas or solid fuel including gas from improved biomass downdraft gasifier
EP3473693A1 (fr) * 2017-10-19 2019-04-24 ThermoDeg s.r.o. Réacteur de dégradation thermique et son procédé de fonctionnement
EP3530717B1 (fr) * 2018-02-21 2023-08-16 ALP Multitech Pvt. Ltd. Procédé de conversion de biomasse agricole ou de déchets biologiques industriels en biocarburant
US10640711B2 (en) 2018-06-05 2020-05-05 Chz Technologies, Llc Multistage thermolysis method for safe and efficient conversion of treated wood waste sources
CN112739457A (zh) * 2018-06-28 2021-04-30 瑞西纳吉公司 用于将烃基废料转化成油气燃料的微波方法
JP6590359B1 (ja) * 2018-07-06 2019-10-16 株式会社翼エンジニアリングサービス バイオマスを原料とする水素製造方法
CN108947173B (zh) * 2018-09-29 2021-03-16 克拉玛依博达生态环保科技有限责任公司 污泥热解装置
EP3956422A1 (fr) * 2019-04-15 2022-02-23 Carbonzero SAGL Dispositif à réacteur continu et procédé de traitement de biomasse
FR3096055B1 (fr) * 2019-05-17 2021-10-22 Inst Polytechnique Grenoble Procédé d’oxydation en bain de sels fondus
FR3103358A1 (fr) * 2019-11-27 2021-05-28 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procédé de nettoyage et d’élimination des tanins présents dans des coques de fruits à coque par torréfaction, Utilisation des coques de fruits à coques torréfiées en tant qu’adsorbants de liquide contaminés.
US11920004B2 (en) 2020-04-01 2024-03-05 Environmental Waste International, Inc. Hybrid processing of waste material
CN115666774A (zh) * 2020-04-24 2023-01-31 不列颠哥伦比亚大学 用于生物质的焙烧和催化热解的流化床反应器系统和方法
CN112194244B (zh) * 2020-08-24 2022-02-11 山东大学 一种水热法镧改性人工湿地生物炭基质及其制备方法
US11578271B1 (en) * 2020-10-30 2023-02-14 Carbon Fiber Recycling, LLC Carbon fiber recycling system and method of operation
RU203231U1 (ru) * 2020-12-22 2021-03-29 Общество с ограниченной ответственностью "Эко-Спектрум" Ротационный инсинератор
CN112961709A (zh) * 2021-02-02 2021-06-15 鹤岗市征楠煤化工有限公司 一种基于含焦油炉尾气的除焦油工艺
WO2022219055A1 (fr) * 2021-04-14 2022-10-20 Rijksuniversiteit Groningen Pyrolyse de biomasse
CN113324415A (zh) * 2021-05-12 2021-08-31 华中科技大学 一种立式霄内热陶粒烧制装置及其使用方法
US11926791B2 (en) * 2021-08-09 2024-03-12 High Plains Biochar LLC Biochar process system
IT202100021575A1 (it) * 2021-08-09 2023-02-09 Archimede S R L "Procedimento per la produzione di combustibili, particolarmente biocombustibili avanzati, da rifiuti organici o scarti biologici"
CN116379436B (zh) * 2023-03-01 2023-10-03 广东顺控环境投资有限公司 一种垃圾焚烧发电用焚烧炉进料装置
CN117417763B (zh) * 2023-11-15 2024-03-22 青岛龙源佰宏机械设备有限公司 一种安全性好的废旧橡塑裂解设备

Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE380035C (de) 1923-09-01 Heinrich Koppers Dr Ing Vorrichtung zur Destillation fester Brennstoffe, insbesondere bei niederen Temperaturen
FR602974A (fr) 1925-04-11 1926-04-06 Saureschutz Ges M B H Procédé pour l'obtention de récipients, appareils et autres objets à l'épreuve des acides
US2723226A (en) 1953-05-04 1955-11-08 Lesher And Associates Inc Low temperature carbonization process
EP0086488A2 (fr) 1982-02-16 1983-08-24 Deutsche Kommunal-Anlagen Miete GmbH Dispositif de déchargement pour four à tambour rotatif
EP0675748A1 (fr) 1992-12-24 1995-10-11 Sea Marconi Technologies Sas Procede de decomposition chimique de composes organiques halogenes.
WO1997007858A1 (fr) 1995-08-25 1997-03-06 Sea Marconi Technologies Di Wander Tumiatti S.A.S. Procede de decontamination et de traitement a contre-courant oxydatif d'une matrice liquide, gazeuse ou solide
CA2351892A1 (fr) 2001-06-29 2002-12-29 Peter B. Fransham Methode de conversion d'une matiere d'alimentation carbonee en liquide, produit de carbonisation et gaz
EP1354172A1 (fr) 2000-12-19 2003-10-22 Sea Marconi Technologies Di Wander Tumiatti S.A.S. Installation destinee au traitement thermique d'une matiere et procede de fonctionnement correspondant
WO2005018841A2 (fr) 2003-08-04 2005-03-03 Colignon, Pascal Thermolyse de dechets organiques en four a billes
DE102005037917A1 (de) 2005-08-11 2007-02-15 Forschungszentrum Karlsruhe Gmbh Verfahren zur Schnellpyrolyse von Lignocellulose
WO2007113311A1 (fr) 2006-04-05 2007-10-11 Bioage Gmbh Tube échangeur de chaleur, reformeur à caloduc comprenant un tel tube échangeur de chaleur et procédé pour utiliser un tel reformeur à caloduc
WO2008005476A2 (fr) 2006-07-06 2008-01-10 Badger Phillip C Procédé et système pour effectuer une pyrolyse éclair ou rapide avec des matières carbonées
WO2008092557A2 (fr) 2007-02-01 2008-08-07 Forschungszentrum Karlsruhe Gmbh Procédé et dispositif permettant de transformer une biomasse en combustible
EP2016159A2 (fr) 2006-04-24 2009-01-21 REW Regenerative Energie Wirtschaftssysteme GmbH Gazéificateur de biomasse et procédé de gazéification allothermique de biomasse
WO2009074268A1 (fr) 2007-12-11 2009-06-18 Forschungszentrum Karlsruhe Gmbh Système de pyrolyse pour matières premières carbonées
WO2009081362A1 (fr) 2007-12-20 2009-07-02 Politecnico Di Torino Procédé de recyclage de déchets organiques permettant de produire des nanotubes de carbone
WO2009138757A2 (fr) 2008-05-14 2009-11-19 Aston University Traitement thermique de biomasse
WO2009138746A1 (fr) 2008-05-14 2009-11-19 Aston University Traitement de biomasse
US20100136463A1 (en) 2000-04-18 2010-06-03 Celltech Power Llc Electrochemical device and methods for energy conversion
US20100209965A1 (en) 2006-07-17 2010-08-19 Bioecon International Holding N.V. Catalytic pyrolysis of fine particulate biomass, and method for reducing the particle size of solid biomass particles
WO2010113129A2 (fr) 2009-03-31 2010-10-07 Chemtex Italia S.R.L. Procédé de prétraitement de biomasse perfectionné
WO2010130988A1 (fr) 2009-05-11 2010-11-18 Aston University Pyrolyse de biomasse

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4140629A (en) * 1977-09-15 1979-02-20 Martco, Inc. Conical screen separator

Patent Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE380035C (de) 1923-09-01 Heinrich Koppers Dr Ing Vorrichtung zur Destillation fester Brennstoffe, insbesondere bei niederen Temperaturen
FR602974A (fr) 1925-04-11 1926-04-06 Saureschutz Ges M B H Procédé pour l'obtention de récipients, appareils et autres objets à l'épreuve des acides
US2723226A (en) 1953-05-04 1955-11-08 Lesher And Associates Inc Low temperature carbonization process
EP0086488A2 (fr) 1982-02-16 1983-08-24 Deutsche Kommunal-Anlagen Miete GmbH Dispositif de déchargement pour four à tambour rotatif
EP0675748A1 (fr) 1992-12-24 1995-10-11 Sea Marconi Technologies Sas Procede de decomposition chimique de composes organiques halogenes.
WO1997007858A1 (fr) 1995-08-25 1997-03-06 Sea Marconi Technologies Di Wander Tumiatti S.A.S. Procede de decontamination et de traitement a contre-courant oxydatif d'une matrice liquide, gazeuse ou solide
US20100136463A1 (en) 2000-04-18 2010-06-03 Celltech Power Llc Electrochemical device and methods for energy conversion
EP1354172A1 (fr) 2000-12-19 2003-10-22 Sea Marconi Technologies Di Wander Tumiatti S.A.S. Installation destinee au traitement thermique d'une matiere et procede de fonctionnement correspondant
CA2351892A1 (fr) 2001-06-29 2002-12-29 Peter B. Fransham Methode de conversion d'une matiere d'alimentation carbonee en liquide, produit de carbonisation et gaz
WO2005018841A2 (fr) 2003-08-04 2005-03-03 Colignon, Pascal Thermolyse de dechets organiques en four a billes
DE102005037917A1 (de) 2005-08-11 2007-02-15 Forschungszentrum Karlsruhe Gmbh Verfahren zur Schnellpyrolyse von Lignocellulose
WO2007113311A1 (fr) 2006-04-05 2007-10-11 Bioage Gmbh Tube échangeur de chaleur, reformeur à caloduc comprenant un tel tube échangeur de chaleur et procédé pour utiliser un tel reformeur à caloduc
EP2016159A2 (fr) 2006-04-24 2009-01-21 REW Regenerative Energie Wirtschaftssysteme GmbH Gazéificateur de biomasse et procédé de gazéification allothermique de biomasse
WO2008005476A2 (fr) 2006-07-06 2008-01-10 Badger Phillip C Procédé et système pour effectuer une pyrolyse éclair ou rapide avec des matières carbonées
US20100209965A1 (en) 2006-07-17 2010-08-19 Bioecon International Holding N.V. Catalytic pyrolysis of fine particulate biomass, and method for reducing the particle size of solid biomass particles
WO2008092557A2 (fr) 2007-02-01 2008-08-07 Forschungszentrum Karlsruhe Gmbh Procédé et dispositif permettant de transformer une biomasse en combustible
WO2009074268A1 (fr) 2007-12-11 2009-06-18 Forschungszentrum Karlsruhe Gmbh Système de pyrolyse pour matières premières carbonées
WO2009081362A1 (fr) 2007-12-20 2009-07-02 Politecnico Di Torino Procédé de recyclage de déchets organiques permettant de produire des nanotubes de carbone
WO2009138757A2 (fr) 2008-05-14 2009-11-19 Aston University Traitement thermique de biomasse
WO2009138746A1 (fr) 2008-05-14 2009-11-19 Aston University Traitement de biomasse
WO2010113129A2 (fr) 2009-03-31 2010-10-07 Chemtex Italia S.R.L. Procédé de prétraitement de biomasse perfectionné
WO2010130988A1 (fr) 2009-05-11 2010-11-18 Aston University Pyrolyse de biomasse

Cited By (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2752445B1 (fr) 2011-08-30 2016-10-19 Carbon Fiber Recycle Industry Ltd. Dispositif et procédé de fabrication de fibres de carbone recyclées
WO2013077748A3 (fr) * 2011-11-21 2013-07-18 Carbonscape Limited Appareil et procédé pour traiter une biomasse
EA027604B1 (ru) * 2011-11-21 2017-08-31 Карбонскейп Лимитед Устройство и способ для обработки биомассы
WO2013110944A1 (fr) * 2012-01-25 2013-08-01 Nov Downhole Eurasia Limited Traitement de matériaux contenant des hydrocarbures
WO2014008496A1 (fr) * 2012-07-06 2014-01-09 South Dakota State University Réacteur de pyrolyse catalytique à lit fluidisé rotatif
CN102758919A (zh) * 2012-07-18 2012-10-31 苏忠 热解旋转滚筒的密封装置
CN102758919B (zh) * 2012-07-18 2015-04-22 苏忠 热解旋转滚筒的密封装置
EP2687782A3 (fr) * 2012-07-21 2015-10-07 Tadeusz Bak Procédé de production d'électricité et de chaleur dans un processus de conversion thermique de différents types de déchets dans une installation intégrée et installation intégrée pour la production d'électricité
ITTO20120894A1 (it) * 2012-10-12 2014-04-13 Sea Marconi Technologies Di Vander Tumiatti S A S Procedimento di co-produzione di bioenergia e prodotti da conversione integrata di biomasse e rifiuti urbani
WO2014057102A1 (fr) * 2012-10-12 2014-04-17 Sea Marconi Technologies Di Vander Tumiatti S.A.S. Procédé de co-production de bio-énergie et de produits à partir de la conversion intégrée de biomasses et de déchets urbains
US20160045841A1 (en) * 2013-03-15 2016-02-18 Transtar Group, Ltd. New and improved system for processing various chemicals and materials
WO2014153570A3 (fr) * 2013-03-15 2015-02-19 Transtar Group, Ltd Système nouveau et amélioré pour le traitement de divers produits chimiques et matériaux
US10899042B2 (en) * 2013-03-28 2021-01-26 Elg Carbon Fibre International Gmbh Pyrolysis system and method of recovering carbon fibres from carbon-fibre-containing plastics
US20190039266A1 (en) * 2013-03-28 2019-02-07 Elg Carbon Fibre International Gmbh Pyrolysis system and method of recovering carbon fibres from carbon-fibre-containing plastics
EP2783764B1 (fr) 2013-03-28 2016-07-13 ELG Carbon Fibre International GmbH Installation de pyrolyse et procédé destinés à la récupération de fibres de carbone à partir de matières synthétiques contenant des fibres de carbone, et fibres de carbone récyclées
EP2789677A1 (fr) * 2013-04-12 2014-10-15 Kymi Baltic Consulting Oü Installation de torréfaction, son fonctionnement et son entretien
WO2014185957A1 (fr) * 2013-05-14 2014-11-20 Ciris Energy, Inc. Traitement de matières premières carbonées
CN105431403A (zh) * 2013-05-14 2016-03-23 克里斯能量有限公司 含碳原料的处理方法
WO2015005807A1 (fr) * 2013-07-12 2015-01-15 Fluid S.A. Procédé de conversion de biomasses en carburant renouvelable et machine destinée à la conversion de biomasses en carburant renouvelable
US9353476B2 (en) 2014-04-18 2016-05-31 Georgia-Pacific Containerboard Llc Method for recycling waste material with reduced odor emission
CN106471101A (zh) * 2014-05-26 2017-03-01 材料开发中心股份公司 用于生产由废弃塑料得到的燃料气体的方法和设备
WO2015181713A1 (fr) * 2014-05-26 2015-12-03 Centro Sviluppo Materiali S.P.A. Procédé et appareil pour la production de gaz combustible obtenu par des plastiques usés
EP3023478A3 (fr) * 2014-11-19 2016-09-21 Embraer , S.A. Un procédé pour le recyclage de matériaux composites et un système pour le traitement de gazes d'échappement
RU2587115C1 (ru) * 2014-12-25 2016-06-10 Открытое акционерное общество "Научно-исследовательский институт металлургической теплотехники" (ОАО "ВНИИМТ") Противоточная шахтная печь для обжига карбонатных материалов, отапливаемая газообразным топливом
AU2020206092B2 (en) * 2019-01-08 2023-08-17 Jie Xiong Jonathan YEO Manufacturing facility
DE102019216564A1 (de) * 2019-10-28 2021-04-29 Siemens Aktiengesellschaft Modulare Abfallbehandlungsanlage
CN111036014A (zh) * 2019-11-22 2020-04-21 中南林业科技大学 人造板干燥系统除尘装置
CN112246832A (zh) * 2020-09-28 2021-01-22 威尔能环保科技(苏州)有限公司 一种电池材料处理系统
WO2022140829A1 (fr) * 2020-12-30 2022-07-07 Petróleo Brasileiro S.A. - Petrobras Système modulaire de traitement d'effluents provenant du nettoyage de coques d'unités flottantes
CN113368857A (zh) * 2021-04-29 2021-09-10 中国环境科学研究院 体相金属间化合物负载催化剂的制备方法
EP4151702A1 (fr) 2021-09-17 2023-03-22 Alpha Trading S.p.A. Procédé de traitement thermique continu d'un flux de matière d'alimentation comprenant au moins une fraction de matière polymère et installation pour la mise en oeuvre de ce procédé

Also Published As

Publication number Publication date
CA2819327A1 (fr) 2012-06-28
EP2655993A2 (fr) 2013-10-30
BR112013015614A2 (pt) 2018-05-15
WO2012085880A3 (fr) 2012-08-23
IT1406771B1 (it) 2014-03-07
ES2691722T3 (es) 2018-11-28
US20130256113A1 (en) 2013-10-03
MX2013007253A (es) 2013-10-01
ITTO20101043A1 (it) 2012-06-24
EP2655993B1 (fr) 2018-07-18

Similar Documents

Publication Publication Date Title
EP2655993B1 (fr) Installation modulaire permettant de réaliser des procédés de conversion de matrices carbonées
CN105505414B (zh) 一种固体垃圾无氧催化热裂解方法
CN101839488B (zh) 一种可燃固体废物回转窑气化焚烧方法
Felix et al. COVID-19 and industrial waste mitigation via thermochemical technologies towards a circular economy: A state-of-the-art review
CN101713304A (zh) 一种生活垃圾湿解预处理干馏气化循环发电的方法
Dabe et al. Technological pathways for bioenergy generation from municipal solid waste: Renewable energy option
CN102430560A (zh) 一种城市生活垃圾综合处理工艺
WO2008014645A1 (fr) Équipement de traitement de déchets de type à protection de l'environnement et à récupération de source d'énergie
CN109679672A (zh) 一种催化热解有机固体废弃物制取气体燃料的反应系统及其方法
US20120200092A1 (en) Systems and Methods for Processing Municipal Wastewater Treatment Sewage Sludge
CN205413887U (zh) 一种医疗废物联合处置系统
CN109513730B (zh) 一种固体有机废弃物真空热解系统与方法
CN104229797A (zh) 热解-活化-燃烧-气化一体炉、垃圾填埋场协调处理系统、活性炭制造方法
CN105710114B (zh) 一种生活垃圾及农林废弃物炭化循环综合处理系统及方法
CN104987871A (zh) 生活垃圾小型化连续式自加热可移动卧式干馏机
Chormare et al. Conversion of solid wastes and natural biomass for deciphering the valorization of biochar in pollution abatement: A review on the thermo-chemical processes
CN101513640A (zh) 锌镉超积累植物无害化固定床热解系统
Pelaez-Samaniego et al. Biomass carbonization technologies
Fodor et al. Municipal solid waste as alternative fuel–minimising emissions and effluents
CN212227043U (zh) 一种固体危险废物资源化利用系统
AU2021202520A1 (en) Valuable materials from solid organic waste (vmw)
CN102776006A (zh) 一种生物质干馏和烘干装置
CN101955778B (zh) 污泥制炭设备及其应用方法
Jeguirim et al. Thermochemical conversion of tomato wastes
CN213019642U (zh) 一种有机废弃物焚烧热解系统

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 11837305

Country of ref document: EP

Kind code of ref document: A2

ENP Entry into the national phase

Ref document number: 2819327

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 13992198

Country of ref document: US

WWE Wipo information: entry into national phase

Ref document number: MX/A/2013/007253

Country of ref document: MX

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 2011837305

Country of ref document: EP

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112013015614

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112013015614

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20130620